СПОСОБ И УСТРОЙСТВО ДЛЯ УМЕНЬШЕНИЯ СОДЕРЖАНИЯ NOxИ N2O В ГАЗАХ

Изобретение относится к способу уменьшения содержания оксидов азота в газах, в частности в технологических и отходящих газах, а также к применяемому для этого устройству. Способ включает пропускание N2O- и NOx-содержащего газа через ряд двух слоев катализатора, содержащих один тип или несколько типов нагруженных железом цеолитов, добавление восстановителя для NOx между этими слоями катализатора, поддержание температуры менее чем 500°С в первом слое катализатора и во втором слое катализатора, поддержание газового давления, по меньшей мере, 2 бар в обоих слоях катализаторов, выбор такой объемной скорости в первом и втором слоях катализатора, что в первом слое катализатора происходит разложение N2O, до содержания не более чем 90% в расчете на содержание N2O на входе первого слоя катализатора и устанавливается содержание N2O более чем 200 частей на млн. и что во втором слое катализатора происходит дальнейшее разложение содержащегося в газе N2O, по меньшей мере, на 30% в расчете на содержание ...

СЕЛЕКТИВНОЕ ПОЛУЧЕНИЕ ПАРА-КСИЛОЛА ПОСРЕДСТВОМ МЕТИЛИРОВАНИЯ ТОЛУОЛА

Изобретение относится к способу селективного получения параксилола, который включает взаимодействие толуола с метанолом в присутствии катализатора, содержащего пористый кристаллический алюмосиликатный цеолит, имеющий параметр диффузии по 2,2-диметилбутану примерно 0,1-15 с-1, измеренный при температуре 120oС и давлении 2,2-диметилбутана (8 кПа). Пористый кристаллический материал предпочтительно представляет собой цеолит со средним размером пор, в частности ZSM-5, который подвергают обработке водяным паром в жестких условиях при температуре, по меньшей мере, 1000oС. Алюмосиликатный цеолитный катализатор предпочтительно объединяют с, по меньшей мере, одним оксидным модификатором, предпочтительно содержащим фосфор, чтобы регулировать снижение объема микропор материала в ходе стадии обработки паром. Технический результат - увеличение выхода продукта, упрощение технологии процесса. 2 с. и 15 з.п. ф-лы, 10 табл., 3 ил.

СПОСОБ КАТАЛИТИЧЕСКОЙ ДЕПАРАФИНИЗАЦИИ И КАТАЛИТИЧЕСКАЯ КОМПОЗИЦИЯ ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

Использование: нефтехимия. Сущность: углеводородное сырье, включающее молекулы парафинов, контактируют в условиях каталитической депарафинизации с каталитической композицией, содержащей кристаллиты металлосиликата, связующий материал и гидрирующий компонент, в котором весовое соотношение кристаллитов металлосиликата и связующего материала находится между 5:95 и 35:65. Кристаллиты металлосиликата обладают кристаллической микропористой структурой и характеризуются тем, что их трехмерная структура построена из тетраэдрических блоков SiO4 и тетраэдрических блоков М или тетраэдрических блоков SiO4 и октаэдрических блоков М, причем эти блоки по углам соединяются через атомы кислорода. М представляет собой Al, Fe, B, Ga или Ti или сочетания этих атомов. Технический результат: снижение газообразования, повышение пористых характеристик каталитической композиции. 2 н. и 19 з.п. ф-лы, 13 табл.

СПОСОБ УДАЛЕНИЯ NOX И N2O ИЗ ОСТАТОЧНОГО ГАЗА ПРОИЗВОДСТВА АЗОТНОЙ КИСЛОТЫ

Изобретение относится к способу понижения концентрации NOx и Na2O в остаточном газе производства азотной кислоты. Способ предусматривает пропускание покидающего абсорбционную колонну остаточного газа перед поступлением на турбину остаточного газа через комбинацию двух стадий. Причем на первой стадии понижают содержание NOx путем каталитического восстановления, на второй стадии понижают содержание N2O в газе путем разложения на азот и кислород, молярное соотношение NOx/N2O перед поступлением газа на вторую стадию находится в интервале от 0,001 до 0,5. На второй стадии газ контактирует с катализатором, который содержит один или более загруженных железом цеолитов, при этом рабочее давление на второй стадии составляет от 4 до 12 бар. 9 з.п. ф-лы, 1 табл, 2 ил.

СПОСОБ КОНВЕРСИИ УГЛЕВОДОРОДОВ С ИСПОЛЬЗОВАНИЕМ СВЯЗАННОГО ЦЕОЛИТОМ ЦЕОЛИТНОГО КАТАЛИЗАТОРА

Использование: в нефтехимии. Сущность: углеводородное сырье контактирует в условиях конверсии углеводородов со связанным цеолитом цеолитным катализатором, включающим (а) первые кристаллы первого цеолита и (б) связующее вещество, содержащее вторые кристаллы второго цеолита, средний размер частиц которых меньше размера первых кристаллов, причем вторые кристаллы находятся в сращенном состоянии с первыми кристаллами и образуют на них покрытие или частичное покрытие. Технический результат - повышение селективности процесса. 50 з.п. ф-лы, 8 табл., 4 ил.

СПОСОБ СНИЖЕНИЯ СОДЕРЖАНИЯ БРОМ-РЕАКЦИОННОСПОСОБНЫХ ЗАГРЯЗНЯЮЩИХ ПРИМЕСЕЙ В АРОМАТИЧЕСКИХ МАТЕРИАЛАХ

Использование: нефтехимия. Сущность: бром-реакционноспособные углеводородные загрязняющие примеси удаляют из ароматических материалов путем подготовки ароматического исходного материала, который характеризуется незначительной концентрацией диенов. Исходный материал вводят в контакт с кислотной активной каталитической композицией в условиях, достаточных для удаления моноолефинов. Ароматический материал может быть предварительно обработан для удаления диенов посредством контактирования этого материала с глиной, катализатором гидрогенизации или гидроочистки в условиях, достаточных для удаления существенной части диенов, но не моноолефинов. Технический результат - повышение продолжительности рабочего цикла. 9 з.п. ф-лы, 2 табл., 2 ил.

СПОСОБ ПОЛУЧЕНИЯ КАТАЛИЗАТОРОВ КАТАЛИТИЧЕСКОГО КРЕКИНГА СО ВЗВЕШЕННЫМ СЛОЕМ С УМЕНЬШЕННЫМИ СКОРОСТЯМИ ИЗНАШИВАНИЯ

Каталитическая микросфера каталитического крекинга со взвешенным катализатором, содержащая цеолит, где указанная микросфера сформирована из пульпы, содержащей: i) каолин, который прокаливали вне его экзотермического перехода; и или ii) кристаллы цеолита, или iii) гидратированный каолин и/или метакаолин, пульпа была смешана с 0.005-0.5 мас.% катионоактивного полиэлектролита относительно массы i) + ii) или i) + iii) перед или во время формирования указанной микросферы. Также представлен способ получения каталитической микросферы. Технический результат - обеспечить катализаторы каталитического крекинга со взвешенным слоем, имеющим улучшенную устойчивость к изнашиванию. 2 н. и 16 з.п. ф-лы, 8 табл., 4 ил., 2 пр.

КАТАЛИЗАТОР ДЛЯ КАТАЛИТИЧЕСКОГО КРЕКИНГА, ЕГО ПОЛУЧЕНИЕ И ИСПОЛЬЗОВАНИЕ

Настоящее изобретение относится к катализатору для каталитического крекинга его получению и использованию. Описан катализатор для каталитического крекинга углеводородных нефтепродуктов, включающий подложку, включающую оксид алюминия и молекулярное сито, имеющий следующее распределение пор: 5-70% пор составляют поры размером <2 нм, 5-70% пор - поры размером 2-4 нм, 0-10% пор - поры размером 4-6 нм, 20-80% пор - поры размером 6-20 нм и 0-40% пор - поры размером 20-100 нм, исходя из объема пор размером не более 100 нм. Описан способ получения катализатора, в котором выполняют следующие стадии: смешивают подложку, включающую оксид алюминия и/или его прекурсоры, с молекулярным ситом, суспендируют и сушат смесь с помощью распылительной сушки, при этом на стадии смешивания вводят расширитель пор, при этом расширитель пор может быть выбран из группы, включающей борную кислоту и соли щелочных металлов, при этом весовое соотношение расширителя пор к подложке составляет 0,1:100-15:100 по весу подложки ...

НОВАЯ МОЛЕКУЛЯРНО-СИТОВАЯ КОМПОЗИЦИЯ ЕММ-12, СПОСОБЫ ЕЕ ПОЛУЧЕНИЯ И ПРИМЕНЕНИЯ

Настоящее изобретение относится к молекулярным ситам, их получению и использованию. Предложен материал EMM-12, имеющий структуру, охарактеризованную в формуле рентгенограммой. EMM-12 в свежеприготовленной и прокаленной формах имеет рентгенограмму, включающую пики, соответствующие дифракционным максимумам в диапазоне от 14,17 до 12,57Å, дифракционным максимумам в диапазоне от 12,1 до 12,56 Å. Материал имеет также неразрешенное рассеивание в интервале от примерно 8,85 до 11,05 Å или не содержащую максимумов область между пиками, соответствующими дифракционным максимумам в диапазоне от 10,14 до 12,0 Å и дифракционным максимумам в диапазоне от 8,66 до 10,13 Å. Согласно изобретению измеренная интенсивность, для которой сделана поправка на уровень фона, в точке с наименьшим значением составляет не менее 50% от значения интенсивности, соответствующей аналогичному межплоскостному расстоянию на линии, соединяющей максимумы в диапазоне от 10,14 до 12,0 Å и в диапазоне от 8,66 до 10,13 Å. Предложен ...

СПОСОБ ПОЛУЧЕНИЯ ШАРИКОВОГО КАТАЛИЗАТОРА КРЕКИНГА

Катализатор получают смешением водной суспензии цеолита Y в натриевой форме с водной суспензией глинозема с размером частиц менее 20 мкм - 100 мас. %, менее 10 мкм - не менее 95 мас.%, менее 4 мкм - не менее 40 мас.%; раствором силиката натрия и раствором сульфата алюминия; формуют гранулы катализатора в колонне с минеральным маслом; проводят активацию раствором сульфата или нитрата аммония, проводят активацию раствором смеси нитратов редкоземельных элементов, отмывают катализатор от солей, сушат и прокаливают в атмосфере дымовых газов и водяного пара. Смесь нитратов РЗЭ содержит нитрата аммония не более 20 мас.% и оксида церия не более 2,5 мас.% на сумму оксидов РЗЭ, а прокаливание катализатора проводят при содержании паров воды 18-30 об. %. Получают катализатор прочностью на раздавливание выше 15 кг/шар с высокой каталитической активностью, пониженной усадкой и малым растрескиванием. 2 табл.

ФОСФОРСОДЕРЖАЩИЙ КАТАЛИЗАТОР ДЛЯ ПРЕВРАЩЕНИЯ ОКСИГЕНАТОВ В ОЛЕФИНЫ

Изобретение относится к способу приготовления фосфорсодержащего катализатора, включающему следующие стадии: (a) экструдирование смеси, которая содержит цеолит и оксид алюминия или гидрат оксида алюминия, в качестве связующего, (b) кальцинирование полученного на стадии (а) экструдата, (c) обработка полученного на стадии (b) кальцинированного экструдата водяным паром, (d) нанесение фосфорсодержащего соединения на обработанный водяным паром экструдат со стадии (с) и (e) кальцинирование модифицированного фосфором экструдата со стадии (d), причем массовая доля фосфора в полученном после стадии (е) катализаторе составляет от 0,8 до 2,5 мас. %. Также изобретение относится к катализатору превращения оксигенатов в олефины, способу получения олефинов из оксигенатов и применению катализатора для превращения оксигенатов в олефины. Получаемый катализатор обладает увеличенным сроком службы при остающейся неизменно селективности и увеличенной степени превращения. 4 н. и 14 з.п. ф-лы, 7 ил., 2 табл., 7 ...

КАТАЛИЗАТОРЫ ГИДРИРОВАНИЯ СО СВЯЗУЮЩИМИ, ИМЕЮЩИМИ НИЗКУЮ ПЛОЩАДЬ ПОВЕРХНОСТИ

Предложены варианты катализаторов депарафинизации углеводородного сырья. Катализаторы депарафинизации включают цеолит, имеющий отношение диоксида кремния к оксиду алюминия 100 или менее, в сочетании со связующим из оксида металла или алюмосиликата. Связующее перед формовкой катализатора имеет площадь поверхности 80 м/г или менее. Нанесенный катализатор имеет отношение площади поверхности цеолита к внешней площади поверхности по меньшей мере 80:100. В одном из вариантов используют цеолит, имеющий поры, образованные 10-членными кольцами. Изобретение обеспечивает катализаторы с высокой активностью для деперафинизации сырья с повышенным содержанием серы и азота. 2 н. и 14 з.п. ф-лы, 5 ил. 1 табл., 8 пр.

СПОСОБ ПОЛУЧЕНИЯ ЦЕОЛИТСОДЕРЖАЩЕГО КАТАЛИЗАТОРА ИСПОСОБ ПЕРЕРАБОТКИ НИЗКООКТАНОВЫХ БЕНЗИНОВЫХ ФРАКЦИЙ

Изобретение может использоваться в нефтеперерабатывающей и нефтехимической промышленности для получения высокооктановых автомобильных бензинов из прямогонных бензиновых фракций. Описан способ получения цеолитсодержащего катализатора для переработки низкооктановых бензиновых фракций на основе ZSM-5, в котором к природному цеолиту клиноптилолит-гейландиту, двукратно обработанному водным раствором NH4Cl, добавляют 2,5-10 мас.% высококремнеземного цеолита ZSM-5 с мольным отношением SiO2/Al2O3=60 и содержанием Na2O не более 0,02 мас.% и дополнительно добавляют 0,5 мас.% ультрадисперсного порошка цинка. Описан также способ переработки низкооктановых бензиновых фракций в присутствии полученного цеолитсодержащего катализатора, причем процесс осуществляют пропусканием паров сырья через стационарный слой катализатора при температуре 300-400°С, атмосферном давлении, объемной скорости подачи сырья 2 ч-1 Технический эффект - повышение содержания в получаемых товарных бензинах алканов изо-строения и ...

СПОСОБЫ ПОЛУЧЕНИЯ КРИСТАЛЛИЧЕСКОГО ЦЕОЛИТА

Описан способ получения кристаллического цеолита из реакционной смеси, содержащей количество воды, достаточное только для того, чтобы, при желании, реакционной смеси можно было бы придать определенную форму. По данному способу реакционную смесь нагревают в условиях кристаллизации и в отсутствие внешней жидкой фазы, так что перед высушиванием кристаллов нет необходимости в удалении избыточной жидкости из закристаллизованного материала. Способ позволяет сократить количество воды для кристаллизации и получить формованные цеолиты без добавления связующего. 2 с. и 40 з.п.ф-лы.

СПОСОБ ГЛУБОКОГО ОКИСЛЕНИЯ ОРГАНИЧЕСКИХ СОЕДИНЕНИЙ

Изобретение относится к области химии и экологии, а именно глубокому окислению органических соединений, которое может быть применено к процессам очистки и обезвреживания газообразных и жидких выбросов, для дожига вредных органических соединений, в том числе летучих, галогенсодержащих и т.п., в отходящих газах. Описан способ глубокого окисления органических соединений, включающий пропускание через слой катализатора потока, содержащего органическое соединение и окислитель, разбавленного инертным газом, отличающийся тем, что в качестве катализатора используют геометрически структурированную систему, включающую микроволокна высококремнеземистого носителя диаметром 5-20 мкм, который характеризуется наличием в инфракрасном спектре полосы поглощения гидроксильных групп с волновым числом ν=3620-3650 сми полушириной 65-75 сми имеет гелеобразный поверхностный слой толщиной от 1 до 500 нм, который характеризуется вязкостью 3000-30000 сП и удельной поверхностью, измеренной методом БЭТ по тепловой десорбции ...

СПОСОБ ПОЛУЧЕНИЯ СИНТЕТИЧЕСКОГО КРИСТАЛЛИЧЕСКОГО АЛЮМОСИЛИКАТА

Изобретение относится к способам получения синтетических кристаллических алюмосиликатов (цеолитов), применяемых в качестве адсорбентов, катализаторов и компонентов моющих составов. Сущность изобретения: смешивают в водно-щелочной среде SiO2 и Al2O3 или их гидраты, или силикаты щелочных металлов и алюминаты щелочных металлов, минерализаторы и при необходимости затравку при следующих мольных отношенияx: SiO2 /Al2O3 = 15-40, ОН-/SiO2 = 0,1-0,2, Н2О/SiO2 = 20-60. 3 з.п. ф-лы, 4 табл., 3 ил.

КАТАЛИЗАТОР СИНТЕЗА ФИШЕРА-ТРОПША И СПОСОБ ЕГО ПОЛУЧЕНИЯ

Изобретение относится к катализаторам синтеза Фишера-Тропша. Описан катализатор синтеза Фишера-Тропша, содержащий носитель из цеолита Hβ и каталитически активное вещество - кобальт, причем носитель дополнительно содержит бемит и представляет собой полые цилиндры с соотношением внутреннего диаметра к внешнему 0,5…3:2…7 мм со следующим составом катализатора (мас.%): кобальт - 10-40; бемит - 6-18; цеолит Hβ - 48-81. Описан способ получения катализатора синтеза Фишера-Тропша, включающий приготовление гранулированного носителя на основе цеолита, нанесение соединения кобальта на прокаленный носитель, просушивание и прокаливание, отличающийся тем, что носитель готовят из смеси цеолита и бемита, а гранулируют путем формования в виде полых цилиндров с соотношением внутреннего диаметра к внешнему 0,5…3:2…7 мм, при этом соотношение ингридиентов находится в следующих пределах (мас.%): кобальт - 10-40; бемит - 6-18; цеолит Hβ - 48-81. Технический результат - получен эффективный катализатор синтеза Фишера-Тропша ...

СПОСОБ КАТАЛИТИЧЕСКОЙ КОНВЕРСИИ УГЛЕВОДОРОДНОГО СЫРЬЯ

Использование: нефтехимия. Сущность: углеводородное нефтяное сырье контактируют катализатором, содержащим цеолит с высоким содержанием двуокиси кремния, содержащим фосфор и редкоземельный элемент и имеющим структуру катализатора пентасил, в реакторе с подвижным катализатором и подвергают каталитическому превращению при температуре от 480 до 680°С и давлении от 1,2 • 105 до 4,0 • 105 Па при времени контакта от 0,1 до 6 с, весовом отношении катализатора к сырью от 4 : 1 до 20 : 1 и весовом отношении пара к сырью от 0,01 : 1 до 0,5 : 1. Технический результат - получение легких олефинов, предпочтительно этилена, пропилена, изобутилена и изоамилена с образованием в качестве побочного продукта высокооктанового бензина. 19 з.п. ф-лы, 9 табл.

СПОСОБ ПОЛУЧЕНИЯ ФЕНОЛА ИЛИ ЕГО ПРОИЗВОДНЫХ

Использование: окислительное гидроксилирование бензола или других ароматических соединений с получением фенола или его производных. Сущность изобретения: фенол или его производные получают газофазным окислительным гидроксилированием бензола или его производных закисью азота при температуре 225-450oС в присутствии предварительно активированного цеолитного катализатора. Активацию ведут при температуре 350-950oC водяным паром или смесью водяного пара с газом-разбавителем при концентрации водяного пара в смеси 3-100% мол. Предпочтительно в качестве разбавителя используют воздух, диоксид углерода, кислород, инертный газ или их смесь. 1 з.п.ф-лы, 4 табл.

СПОСОБ IN-SITU ПОЛУЧЕНИЯ КАТАЛИЗАТОРА ДЛЯ ПОЛУЧЕНИЯ ПО МЕНЬШЕЙ МЕРЕ ОДНОГО ИЗ ТОЛУОЛА, ПАРА-КСИЛОЛА И НИЗШИХ ОЛЕФИНОВ, А ТАКЖЕ ПРОЦЕСС РЕАКЦИИ

Настоящее изобретение относится к способу in-situ получения катализатора для получения по меньшей мере одного из толуола, пара-ксилола и низших олефинов, а также к процессу реакции получения по меньшей мере одного из толуола, пара-ксилола и низших олефинов, и относится к области химической технологии. Описан способ in-situ получения катализатора, в котором модификатор приводят в контакт с цеолитным молекулярным ситом в реакторе для in-situ получения катализатора для получения пара-ксилола, толуола и/или низших олефинов из сырьевого материала, содержащего метанол и/или диметиловый эфир; и реактор представляет собой реактор для получения пара-ксилола, толуола и/или низших олефинов из сырьевого материала, содержащего метанол и/или диметиловый эфир; при этом модификатор содержит по меньшей мере один из следующих модификаторов: Модификатор I: фосфорсодержащий реагент и силилирующий реагент; Модификатор II: силилирующий реагент; Модификатор III: силилирующий реагент и водяной пар; Модификатор ...

СПОСОБ ОКИСЛЕНИЯ БЕНЗОЛА В ФЕНОЛ

Изобретение относится к способу получения фенола путем прямого газофазного окисления бензола закисью азота в присутствии промышленных цеолитов. Окисление бензола в фенол проводят при 350-450oС закисью азота в присутствии высококремнеземного цеолитного катализатора, модифицированного добавками ионов металлов. Пропитку ведут водными растворами солей металлов по влагоемкости цеолита, предварительно прокаленного при 500-550oС и затем активированного прокаливанием при высокой температуре. В качестве добавок используют ионы натрия, кальция, бария, стронция, марганца, хрома и сурьмы или их смеси, в качестве цеолита - ZSM-5-50 и ZSM-5-80. Активацию катализатора проводят в две стадии, на первой из которых катализатор прокаливают в токе воздуха при 450-500oС, а на второй при 700-900oС. Объемное отношение бензол : закись азота = 1:(1,7-2,2). Технический результат - повышение селективности процесса и выхода фенола. 3 з.п. ф-лы, 1 табл.

ПОВЫШЕНИЕ АКТИВНОСТИ ЦЕОЛИТНОГО КАТАЛИЗАТОРА ФОСФАТОМ АЛЮМИНИЯ И ФОСФОРОМ

... 1. Способ повышения каталитической активности кислотного цеолита с малыми и средними порами, который включает стадии обработки по меньшей мере одного кислотного цеолита с малыми или средними порами 0,5-10 мас. % соединения фосфора с получением обработанного фосфором цеолита и совмещения этого обработанного фосфором цеолита с 1-50 мас. % AlР04 в пересчете на массу цеолита. 2. Способ по п. 1, в котором соединение фосфора выбирают из группы, включающей вторичный кислый фосфат аммония, первичный кислый фосфат аммония, фосфорную кислоту, ее кислые соли, полифосфорную кислоту и ее кислые соли, органические фосфиты и органофосфины. 3. Способ по п. 1, в котором подвергаемый обработке фосфором цеолит характеризуется типом структуры, выбранным из группы, включающей MFI, MEL, MTW, EUO, MTT, FER, MFS, TON, СНА, ERI, MAZ, OFF, RHO, HEV, KFI, LEV и LTA. 4. Способ по п. 1, в котором подвергаемый обработке фосфором цеолит выбирают из группы, включающей ZSM-5, ZSM-11, ZSM-22, ZSM-23, ZSM-34, ZSM-35. ZSM ...

СПОСОБ ПРОИЗВОДСТВА ЛЕГКИХ ОЛЕФИНОВ КАТАЛИТИЧЕСКОЙ КОНВЕРСИЕЙ УГЛЕВОДОРОДОВ

... 1. Способ каталитической конверсии углеводородов нефти, отличающийся тем, что предварительно нагретые углеводороды нефти контактируют с цеолитом с высоким содержанием двуокиси кремния, содержащим фосфор и редкоземельный элемент и имеющим структуру катализатора пентасил, в реакторе с подвижным катализатором и затем подвергаются каталитической конверсии при температуре от 480 до 680°С и давлении от 1,2 • 105 до 4,0 • 105 Па при времени контакта от 0,1 до 6 с, весовом отношении катализатора к сырью от 4 : 1 до 20 : 1 и весовом отношении пара к сырью от 0,01 : 1 до 0,5 : 1. 2. Способ по п. 1, отличающийся тем, что указанную каталитическую конверсию проводят при температуре от 500 до 620°С при времени контакта от 0,1 до 6 с, весовом отношении катализатора к сырью от 5 : 1 до 15 : 1, и весовом отношении пара к сырью от 0,05 : 1 до 0,3 : 1. 3. Способ по п. 1, отличающийся тем, что указанный реактор с подвижным катализатором представляет собой реактор с восходящим потоком. 4. Способ по п. 1, отличающийся ...

КАТАЛИТИЧЕСКАЯ КОМПОЗИЦИЯ И СПОСОБ ТРАНСАЛКИЛИРОВАНИЯ АРОМАТИЧЕСКИХ УГЛЕВОДОРОДОВ

... 1. Каталитическая композиция, включающая цеолит и неорганическое связующее вещество, где цеолит имеет кристаллическую структуру с отверстиями, образованными 12 тетраэдрами, а связующим веществом является γ-оксид алюминия, при этом указанная композиция отличается объемом пор, получаемым при суммировании присутствующих в указанной каталитической композиции мезопористой и макропористой составляющих, превышающим или равным 0,7 см3/г, причем по меньшей мере 30% указанного объема состоит из пор, диаметр которых более 100 нм. 2. Каталитическая композиция по п.1, прочность на раздавливание которой больше или равна 1,7 кг/мм. 3. Каталитическая композиция по п.1, кажущаяся плотность которой не превышает 0,5 г/ см3. 4. Каталитическая композиция по п.1 в виде частиц, имеющих диаметр не менее 1,8 мм. 5. Каталитическая композиция по п.4 в виде частиц, имеющих диаметр не менее 2,0 мм. 6. Каталитическая композиция по п.1 в виде цилиндрических гранул. 7. Каталитическая композиция по п.1, в которой цеолит ...

СПОСОБ ПРИГОТОВЛЕНИЯ КАТАЛИЗАТОРА ДЛЯ КРЕКИНГА НЕФТЯНЫХ ФРАКЦИЙ

... 1. СПОСОБ ПРИГОТОВЛЕНИЯ КАТАЛИЗАТОРА ДЛЯ КРЕКИНГА НЕФТЯНЫХ ФРАКЦИЙ и дожига оксида углерода в процессе регенерации катализатора, включающий смешение водной суспензии цеолита NaI, водного раствора сульфата алюминия и водного раствора силиката натрия, коагуляцию и/или синерезис, активацию нитратом или сульфатом аммония, промывку полученного гидрогеля, введение нитратов редкоземельных элементов и платинохлористоводородной кислоты, сушку, прокаливание, отличающийся тем, что, с целью получения катализатора с повышенной активностью в процессе дожига оксида углерода и упрощения технологии его приготовления, введение нитратов редкоземельных элементов осуществляют в водную суспензию цеолита NaI и введение платинохлористоводородной кислоты осуществляют в водный раствор сульфата алюминия. 2. Способ по п.1, отличающийся тем, что, с целью получения катализатора в микросферической форме, промытый гидрогель подвергают диспергации, распылительной сушке и прокаливанию.

АЛЮМОСИЛИКАТНАЯ ШПИНЕЛЬ И СПОСОБ ЕЕ ПОЛУЧЕНИЯ

... 1. Алюмосиликатная шпинель состава 3,3 Al2О3•SiО2 структурного типа j-Al2О3 в качестве катализатора и/или носителя. 2. Способ получения алюмосиликатной шпинели состава 3,3 Al2О3•SiО2 структурного типа j- Al2О3, заключающийся в механической активации смеси гидроксида алюминия и оксида кремния при энергонапряженности 3-210 Вт/г в течение 0,08-3 ч с последующей термообработкой при 700-1100oC в течение 1-12 ч.

СПОСОБ КРЕКИНГА НЕФТЯНЫХ ФРАКЦИЙ

Изобретение относится к области нефтеперерабатывающей промышленности, а именно к способам получения легких олефинов. Предлагаемый способ крекинга нефтяных фракций включает подачу нефтяных фракций в реактор с псевдоожиженным слоем катализатора при температуре 540-640°С и причем используемый катализатор содержит модифицированный фосфором цеолит ZSM-5 с отношением Si/Al от 40 до 150 и содержанием фосфора от 1,0 до 4,0 мас.%, в качестве компонентов матрицы - оксид алюминия и бентонитовую глину или оксид алюминия, бентонитовую глину и аморфный алюмосиликат при следующем соотношении компонентов в катализаторе, мас.%: модифицированный фосфором цеолит ZSM-5 40-50; оксид алюминия 15-25; бентонитовая глина 20-35 и аморфный алюмосиликат 0-10. Технический результат - создание способа крекинга нефтяных фракций, обеспечивающего повышение выхода легких олефинов. 1 з.п. ф-лы, 2 табл., 9 пр.

СПОСОБ КОНВЕРСИИ УГЛЕВОДОРОДОВ, КАТАЛИЗАТОР ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ С МИКРО-МЕЗОПОРИСТОЙ СТРУКТУРОЙ ИСПОСОБ ПРИГОТОВЛЕНИЯ КАТАЛИЗАТОРА

Группа изобретений относится к конверсии углеводородов с использованием катализаторов с микро-мезопористой структурой. Предлагается способ конверсии углеводородов, включающий введение углеводородного сырья в условиях конверсии углеводородов в контакт с катализатором с микро-мезопористой структурой, содержащим микропористые кристаллические силикаты с цеолитной структурой состава Т2O3(10-1000)SiO2, где Т - элементы, выбранные из группы, состоящей из р-элементов III группы или d-элементов IV-VIII группы, или их смеси, при этом микро-мезопористая структура характеризуется долей микропор от 0,03 до 0,40 и долей мезопор от 0,60 до 0,97. Катализатор готовят суспендированием микропористых кристаллических силикатов с цеолитной структурой названного состава в щелочном растворе с концентрацией гидроксид-ионов 0, 2-1,5 моль/л до достижения остаточного содержания цеолитной фазы в суспензии 3-40 мас.%. В полученную суспензию силиката вводят раствор катионного поверхностно-активного вещества в виде соли ...

СПОСОБ ПОЛУЧЕНИЯ МЕТАЛЛООБМЕННЫХ ЦЕОЛИТОВ ПОСРЕДСТВОМ ИОННОГО ОБМЕНА В ТВЁРДОМ СОСТОЯНИИ ПРИ НИЗКИХ ТЕМПЕРАТУРАХ

СПОСОБ ПОЛУЧЕНИЯ КАРБОНОВОЙ КИСЛОТЫ

Алифатическая карбоновая кислота, содержащая n+1 углеродных атомов, где n - целое число до 6, может быть получена введением алифатического спирта, содержащего n углеродных атомов, или его реакционноспособного производного в контакт с моноокисью углерода в присутствии морденитного цеолитного катализатора, содержащего медь, никель, иридий, родий или кобальт, при повышенной температуре и давлении в интервале от 15 до 200 бар.

СПОСОБ ПОЛУЧЕНИЯ ШАРИКОВОГО КАТАЛИЗАТОРА КРЕКИНГА

Способ получения шарикового цеолитсодержащего катализатора крекинга нефтяных фракций, включающий смешение водной суспензии цеолита Y в обмененной катионной форме с водной суспензией наполнителя, раствором силиката натрия и раствором сульфата алюминия, формование гранул катализатора в колонне с минеральным маслом, активацию раствором сульфата алюминия, активацию раствором смеси нитратов редкоземельных элементов, отмывку от солей, сушку и прокалку в атмосфере дымовых газов и водяного пара, отличающийся тем, что в качестве наполнителя используют глинозем с содержанием α-Al2О3 не более 85 мас.%, и θ-Al2О3 10-20 мас.%, и указанный глинозем используют в виде суспензии в растворе силиката натрия.

ЦЕОЛИТНЫЕ КАТАЛИЗАТОРЫ, СТОЙКИЕ К НАТРИЮ, И СПОСОБЫ ИХ ПОЛУЧЕНИЯ

... 1. Катализатор содержащий(a) цеолит,(b) соединение иттрия и(c) натрий, причем количество натрия, присутствующего в катализаторе, составляет, по меньшей мере, 18,6 мкг на квадратный метр площади поверхности цеолита.2. Катализатор по п. 1, где цеолит представляет собой фожазит.3. Катализатор по п. 1, где цеолит выбран из группы, состоящей из цеолита типа Y, цеолита типа Х типа, цеолита Бета и их термически обработанных производных.4. Катализатор по п. 1, где цеолит представляет собой цеолит типа Y.5. Катализатор по п. 1, в котором натрий присутствует в количестве в диапазоне от 22 до 50 мкг на квадратный метр площади поверхности цеолита.6. Катализатор по п. 1, в котором иттрий вводят обменом в цеолит, причем иттрий присутствует в катализаторе в количестве в диапазоне от 0,5 до 15 мас.% в расчете на цеолит.7. Катализатор по п. 1, дополнительно содержащий матрицу неорганического оксида.8. Катализатор по п. 7, в котором матрица неорганического оксида содержит соединение, которое выбирают из ...

НОВЫЙ УЛЬТРАСТАБИЛЬНЫЙ ЦЕОЛИТ Y И СПОСОБ ЕГО ПОЛУЧЕНИЯ

... 1. Способ получения ультрастабильного цеолита Y (USY), содержащий(a) нагревание аммонийобменного цеолита Y с целью получения цеолита USY;(b) добавление цеолита USY в аммонийобменную ванну и обработка содержимого ванны, включающего цеолит USY, в гидротермальных условиях; и(c) выделение цеолита USY, характеризующегося содержанием натрия 2% или менее в пересчете на NaO.2. Способ по п.1, в котором USY, полученный на стадии (а), содержит натрий в виде NaO в количестве 5 мас.% или менее от массы цеолита USY.3. Способ по п.1, в котором способ дополнительно содержит осуществление обмена USY, полученного на стадии (а), с аммониевой солью до гидротермальной обработки USY в соответствии со стадией (b).4. Способ по п.1, в котором цеолит USY, выделенный на стадии (с), содержит натрий в виде NaO в количестве 1 мас.% или менее от массы цеолита Y марки USY.5. Способ по п.1, в котором цеолит USY, выделенный на стадии (с), содержит натрий в виде NaO в количестве 0,5 мас.% или менее от массы цеолита USY.6 ...

СПОСОБ ПОЛУЧЕНИЯ ВЫСОКООКТАНОВОГО БЕНЗИНА

Способ получения высокооктанового бензина риформингом бензиновых фракций в присутствии цеолитсодержащего катализатора при повышенной температуре и атмосферном давлении с использованием предварительной обработки катализатора раствором модификатора - комплексами производного силоксана с металлами, отличающийся тем, что предварительную обработку проводят путем пропускания раствора модификатора через катализатор с объемной скоростью 0,5-1,5 см/см•с при температуре 70-80С, в течение 1-3 ч, при этом скорость подачи раствора модификатора выдерживают большие скорости испарения.

ТИТАН-СОДЕРЖАЩИЙ ЦЕОЛИТ, СПОСОБ ЕГО ПОЛУЧЕНИЯ (ВАРИАНТЫ), СПОСОБ ЭПОКСИДИРОВАНИЯ ОЛЕФИНОВ, ПРОИЗВОДНЫЕ БЕНЗИЛ-ЗАМЕЩЕННОГО АММОНИЯ

Предложено кристаллическое молекулярное сито, имеющее матричную структуру, изоморфную структуре бета цеолита, и содержащее Si и Ti, но не содержащее решеточного Al, этот цеолит может эффективно катализировать эпоксидирование олефинов при использовании в качестве окисляющего агента перекиси водорода или органической гидроперекиси.

КАТАЛИТИЧЕСКИЕ КОМПОЗИЦИИ МОЛЕКУЛЯРНОГО СИТА, КАТАЛИТИЧЕСКИЕ КОМПОЗИТЫ, СИСТЕМЫ, И СПОСОБЫ

ПРИМЕНЕНИЕ КРИСТАЛЛИЧЕСКИХ АЛЮМОСИЛИКАТОВ (ЦЕОЛИТОВ), СОДЕРЖАЩИХ КИСЛОТНЫЕ ЦЕНТРЫ ИЗ ИОНОВ ОКИСЛОВ ЛИТИЯ, НАТРИЯ, РУБИДИЯ, ЦЕЗИЯ ДЛЯ КАТАЛИЗА РЕАКЦИИ ПРЯМОГО ПРИСОЕДИНЕНИЯ СИНИЛЬНОЙ КИСЛОТЫ К АЦЕТИЛЕНУ С ЦЕЛЬЮ ПОЛУЧЕНИЯ АКРИЛОНИТРИЛА

... 1. Кристаллический алюмосиликат, содержащий следующее соотношение ингредиентов, вес.%: окись лития 7,19; окись алюминия 24,46; окись кремния 68,35 используется для катализа реакции прямого присоединения синильной кислоты к ацетилену с целью получения акрилонитрила. ! 2. Кристаллический алюмосиликат, содержащий следующее соотношение ингредиентов, вес.%: окись натрия 13,81; окись алюминия 22,72; окись кремния 63,47 используется для катализа реакции прямого присоединения синильной кислоты к ацетилену с целью получения акрилонитрила. ! 3. Кристаллический алюмосиликат, содержащий следующее соотношение ингредиентов, вес.%: окись калия 19,54; окись алюминия 21,21; окись кремния 59,25 используется для катализа реакции прямого присоединения синильной кислоты к ацетилену с целью получения акрилонитрила. ! 4. Кристаллический алюмосиликат, содержащий следующее соотношение ингредиентов, вес.%: окись рубидия 32,58; окись алюминия 17,77; окись кремния 49,65 используется для катализа реакции прямого присоединения ...

Способ получения биотоплива из осадков сточных вод

Настоящее изобретение относится к способу получения биотоплива из осадков сточных вод, а именно осадка первичных отстойников и обезвоженного избыточного активного ила в чистом виде или смешанных в любом соотношении, заключающемуся в том, что биотопливо производится из осадков сточных вод в процессе гидротермального ожижения в реакторе периодического действия, отличающемуся тем, что для конверсии используют катализатор, состоящий из минеральной цеолитной декатионизированной матрицы, импрегнированной ионами никеля и меди в количестве 4 и 3% соответственно от массы минеральной матрицы при соблюдении следующих параметров процесса: доза биомассы по сухому веществу 1:15-1:5, температура 250-280°С, давление 3,5-6 МПа, доза катализатора 10-15% от массы осадка сточных вод в пересчете на сухое вещество. Настоящее изобретение обеспечивает увеличение выхода биотоплива при переработке осадков сточных вод методом гидротермального ожижения. 1 ил., 2 табл., 3 пр.

Способ повышения каталитической активности алюмосиликатных катализаторов

Способ каталитического крекинга и алкилирования углеводородов

Способ получения гранулированных цеолитных катализаторов

Способ повышения активности алюмосиликатного катализатора крекинга

СПОСОБ ПОЛУЧЕНИЯ ШАРИКОВОГО АЛЮМОСИЛИКАТНОГО, В ТОМ ЧИСЛЕ ЦЕОЛИТСОДЕРЖАЩЕГО, КАТАЛИЗАТОРА КРЕКИНГА

Катализатор для газофазной дегидратации пиридилэтанолов в винилпиридины

Катализатор для неполного оксиления пропана

Катализатор крекинга нефтяных фракций

Способ очистки газов от сернистых соединений

Изобретение относится к процессам каталитической очистки газов от сернистых соединений и позволяет повысить стабильность процесса при сохранении активности катализатора на высоком уровне. Для осуществления очистки ведут контактирование газа, содержащего сернистые соединения, с алюмокобальтмолибденовым катализатором для гидрирования сернистых соединений до сероводорода, а затем газ пропускают через катализатор, содержащий окислы железа или молибдена, или меди, или палладия, при содержании металла 0,5-19 мас.% в прокаленном катализаторе, нанесенные на окислы титана или циркония, или кремния, или алюминия, причем в случае присутствия палладия в катализаторе отношение числа атомов металла к числу атомов палладия составляет 20-1000. 1 табл. СО i со 4 СО ...

Катализатор для парофазного нитрования ароматических соединений

Изобретение касается каталити- честсой химии, в частности состава катализатора для парофазного нитрования ароматических соединений (КТН). Повьппение активности КТН достигается за счет его определенного качественного и количественного состава. В КТН входят следующие компоненты, мас.%: трехокись серы 5,1-40 и остальное глинозем или кремнезем, или их смесь в массовом соотношении 1:(1-9,6)., Кроме того, состав КТН дополнительно может содержать следу- юоще компоненты, мас.%: окись кобальта 16,5 или его смесь с окисью молибдена 13,5-19,5, или смесь окиси никеля и окиси вольфрама 17,6 и остальное глинозем или кремнезем, или их смесь в массовом соотношении 1:3:7 и трехокись серы в количестве 5,1- 14,6% от массы указанной смеси окислов металлов с глиноземом и/или кремнеземом. Испытания КТН в процессе нитрования ароматического соединения , например толуола, дают кон- .версию 24,8% при 174 С 4 ч, селективность по о- и п-нитротолуолу 55,2 и 44,8%. 1 з.п. ф-лы. 3 табл. СО ...

Каталитическая композиция для дегидроциклодимеризации С @ -С @ -алифатических углеводородов и способ их дегидроциклодимеризации

Изобретение относится к каталитической композиции для дегидроциклодимеризации C2- C4алифатических углеводородов и способу их дегидроциклодимеризации. С целью повышения стойкости к закоксовыванию каталитической композиции, она включает следующее соотношение компонентов, мас.%: галлий 0,6 - 1,2 компонент, содержащий оксид алюминия 44,0 - 51,8 цеолит ZSM-типа остальное (с отношением диоксида кремния к оксиду алюминия 32,2 - 71,2. В качестве компонента композиция включает фосфорсодержащий оксид алюминия при массовом отношении фосфора к алюминию 0,21 - 1,0. Получение ароматических углеводородов с 2 - 4 атомами углерода дегидроциклодимеризацией C2- C4-алифатических углеводородов ведут путем контактирования углеводородов при 532 - 545°С, давлении 103 - 517 кПа и часовой объемной скорости 0,8 - 2 ч-1с катализатором указанного состава. 1 табл.

Катализатор для очистки выхлопных газов от окислов азота

Способ получения цеолитсодержащего микросферического катализатора крекинга

VERFAHREN ZUR HERSTELLUNG VON DIMETHYLAMIN

VERFAHREN ZUR HERSTELLUNG VON MOLEKULARSIEBSCHICHTEN

Verfahren zur Entfernung von Stickstoffoxiden aus Abgasen

Verwendung eines Katalysators zur Verringerung der Partikelmenge und/oder -größe im Dieselabgas

VERFAHREN ZUR ALKYLIERUNG BENZO-REICHER REFORMIERUNGSPRODUKTE MITTELS MCM-49

Verfahren zur Reduktion von in Abgasen enthaltenen Stickoxiden mittels eines zeolithhaltigen Katalysators

VERFAHREN ZUM AUFTRAGEN VON MOLEKULARSIEBEKRISTALLEN AUF EINEN TRÄGER UND DER DAMIT ERHALTENE BESCHICHTETE TRÄGER

PROCESS FOR PREPARING CATALYTIC CRACKING CATALYSTS

VERFAHREN ZUR HERABSETZUNG DER MENGE AN SCHWEFELOXIDEN IN INSBESONDERE BEI EINEM CRACKVERFAHREN ANFALLENDEN GASGEMISCHEN, UND STOFFGEMISCH ZU DEREN DURCHFUEHRUNG

ISOPARAFFIN/OLEFIN-ALKYLIERUNG MIT MIKROPRÖSEM MCM-MATERIAL UNTER ÜBERKRITISCHEN BEDINGUNGEN DES ISOPARRAFINS

PRODUKTION VON SCHMIERMITTELN MIT HOHEM VISKOSITÄTSINDEX

PRODUCTION OF AROMATICS FROM ETHANE AND/OR ETHYLENE

VERFAHREN ZUR HERSTELLUNG HOCHPOROESER KUGELFOERMIGER ZEOLITHHALTIGER ALUMINIUMOXIDKOERPER

KATALYSATOR ZUR UMWANDLUNG VON KOHLENWASSERSTOFFVERBINDUNGEN UND VERFAHREN ZUR SELEKTIVEN HERSTELLUNG VON MITTELOELEN.

Uran, mindestens einem Promotor für Uran und mindestens ein Edelmetall enthaltender Multifunktionskatalysator für die Behandlung von Abgasen der Verbrennungsmotoren und dessen Herstellung.

Kristalline Aluminophosphate und verwandte Verbindungen.

KIESELSAEURE-MAGNESIUMHYDROXID ALS KATALYSATORBASIS.

Hydrocracking a hydrocarbon charge uses a catalyst containing an amorphous or poorly crystallized matrix of the oxide type and an IM-5 zeolite, a hydrogenating-dehydrogenating element, and boron or silicon as promoter

Process for hydrocracking a hydrocarbon charge comprises contacting the charge with a catalyst containing an amorphous or poorly crystallized matrix of the oxide type and an IM-5 zeolite, a hydrogenating-dehydrogenating element consisting of a group VIII or group VIB metal, and boron or silicon as promoter. Independent claims are also included for: (1) a catalyst for hydrocracking a hydrocarbon charge comprising 0.1-99.7 (wt.%) IM-5 zeolite, 0.1-60 hydrogenating-dehydrogenating metal, 0.1-99 matrix, 0.1-20 boron or silicon, 0-20 phosphorus, 0-20 group VIIA metal, 0-20 group VIIB metal, and 0-60 group VB; and (2) a process for the production of the catalyst comprising: (a) forming a precursor by molding a matrix, IM-5 zeolite, a group VIB metal, a group VIII metal, boron or silicon as promoter, phosphorus, and a group VIIA metal; (b) calcining at at least 150O C; (c) impregnating the precursor obtained in (b) with a solution containing an element selected from a group VIIB, VB, VIII, VIB ...

Selective hydrogenation of olefins in naphthas - using three-component catalyst and single stage operation

Process and three-component catalyst system for selective hydrogenation of olefins in hydrocarbon mixts. contg. aromatics comprising (a) an inorganic non-crystalline support component, (b) 10-70 (10-30)% wt. crystalline aluminosilicate component with silica to alumina mole ratio >=2.5 and alkali metal content 2.0% wt. (as oxide), and (c) 1-25% wt (based on (a) component) transition metal hydrogenation component (Group VIB or VIII metal and/or oxide and/or sulphide, pref. chosen from Ni, Mo and/or W). Pref. component (a) is alumina, or silica-stabilised alumina or magnesia, where pref. silica to alumina (or magnesia) ratio is 1:4-6. Process operating conditions are 150-700 degrees F, (pref. inlet 200-280 degrees F, outlet 450-650 degrees F) 100-1000 (400) psign. H2 feed rate > 500 (>1000) SCF/B, and contact time 0.25-8 hrs (pref. 1-2). Catalyst and processis esp. suitable for hydrogenation of olefins in gasoline range materials.

Verfahren zur Alkylierung in der Gasphase mit gespaltener Katalysatorbeladung

Kontinuierliches Verfahren zur katalytischen Umwandlung von organischen Einsatzmaterialien

ALUMINIUM-MODIFIZIERTE KIESELSAEURE, VERFAHREN ZU DEREN HERSTELLUNG UND DEREN VERWENDUNG

KATALYSATOR ZUR HYDROBEHANDLUNG HOCHSIEDENDER KOHLENWASSERSTOFFFRAKTIONEN

A PROCESS FOR CONVERTING SYNTHESIS GAS TO HYDROCARBONS

PROCESS FOR THE PRODUCTION OF CATALYSTS BASED ON CRYSTALLINE ALUMINOSILICATES AND THE USE OF CATALYSTS SO-PRODUCED

PROCESS FOR THE PREPARATION OF AN AROMATIC HYDROCARBON MIXTURE, AND AROMATIC HYDROCARBON MIXTURES SO PREPARED

VERFAHREN ZUR HERSTELLUNG VON BORHALTIGEN ALUMOSILIKATEN MIT PENTASILSTRUKTUR

PROCESS FOR THE PREPARATION OF 4-PENTENOIC-ACID ESTERS

VERBESSERTES FLEXIBELES VERFAHREN ZUR HERSTELLUNG VON BASISÖLEN UND MITTELDESTILLATEN MITTELS EINER HYDROISOMERIERUNG UND ANSCHLIESSENDER KATALYTISCHEN ENTPARRAFFINIERUNG

SELECTIVE DEALUMINATION OF ZEOLITES

Verfahren zur Herstellung eines formselektiven kristallinen Aluminiumsilikat-Katalysators mit Hydrierungs-Dehydrierungs-Aktivitaet und Anwendung des Katalysators zur Umsetzung eines organischen Beschickungsmaterials

IMPROVEMENTS RELATING TO CATALYSTS AND THE USE THEREOF

... 1,248,435. Hydrocracking catalysts. TEXACO DEVELOPMENT CORP. 22 Oct., 1968 [27 Oct., 1967], No. 49950/68. Heading B1E. [Also in Division C5] A hydrocracking catalyst comprises (1) a hydrogenating component which comprises at least one metal selected from Group VI and Group VIII and (2) a cracking component which consists essentially of a mixture of (a) amorphous inorganic oxide material selected from silica, alumina, zirconia, magnesia and mixtures thereof and (b) crystalline zeolite having an alkali metal content (calculated as the oxide) of not greater than 1.0 weight per cent, the zeolite constituting from 5 to 55 weight per cent of the cracking component and the rare earth metal content of the cracking component being less than 0.1 weight per cent. The metal selected from Group VI and Group VIII may be chromium, molybdenum, tungsten, cobalt, nickel or a metal of the palladium and platinum triads, for example palladium, and may be in the form of elemental metal, oxide, sulphide or a ...

Catalytic conversion of hydrocarbons

A process for cracking a hydrocarbon fraction boiling in the range 400-850 DEG F. comprises use of a catalyst containing (a) nickel, tungsten or compounds thereof; (b) an acidic inorganic oxide in amorphous form selected from SiO2, Al2O3, MgO, ZrO2, or mixtures; and (c) a crystalline zeolite. Typical cracking conditions are: pressure 500-10,000 p.s.i.g.; Hydrogen rate 1000-20,000 SCF/B.; space velocity 0.1-10v./v./hr. Comparative examples describe the cracking of gas oil.ALSO:A hydrocarbon conversion catalyst comprises a crystalline zeolite and an amorphous acidic in-organic oxide of SiO2, Al2O3, MgO, ZrO2 or mixtures which support a metal or compound thereof selected from nickel, tungsten or compounds thereof. Zeolites A, D, X, Y, inordenite, charazite and analcite are specified. Preferred compounds of Ni and W are the oxides and sulphides.

Selective Conversion Process

... 1,178,427. Cracking catalysts. ESSO RESEARCH & ENG. CO. 26 May, 1967 [7 June, 1966], No. 24595/67. Heading B1E. [Also in Divisions Cl and C5] A catalyst for selectively hydrocracking straight-chain hydrocarbons contained in a hydrocarbon feedstock comprises a rare earth metal-containing crystalline aluminosilicate zeolite having uniform pore openings of less than 6 Angstrom units. The zeolite may be zeolite A or natural or synthetic erionite. It may be base-exchanged with a rare earth metal. Rare earth metals are defined as those having atomic numbers from 57 to 71 inclusive, scandium and yttrium. The catalysts may also contain cadmium or zinc. A hydrogenation metal component such as cobalt, nickel, platium, palladium, ruthenium, rhodium, osmium or iridium in the form of the free metal, oxide, sulphide or mixtures thereof may also be included.

ISOMERIZATION OF BUTENE-1 TO CIS-BUTENE-2

... 1326059 Isomerizing butene-1 to butene-2 PETRO-TEX CHEMICAL CORP 5 Nov 1970 [24 Nov 1969] 52753/70 Heading C5E Butene-1 is isomerized to butene-2 (mainly cis) by contact in the liquid phase at a feed rate of 5-15 LHSV with a molecular sieve catalyst of effective pore size of from more than 5 to 8Š which has been activated by heating to at least 300‹ C. The molecular sieve is preferably of the X-type. The isomerization may be effected at 50-150‹ C. under a pressure sufficient to maintain the butene in the liquid phase. The used catalyst may be regenerated by heating to 400-600‹ C. in a non-reactive atmosphere. Other hydrocarbons such as n-butane and butene-2 may be present in the feed.

Catalytically upgrading sulphur rich naphtha

Methods for optimizing Fischer-Tropsch synthesis of hydrocarbons in the distillate fuel and/or lube base oil ranges

A method for optimising the conversion of syngas to higher molecular weight hydrocarbons boiling in the distillate fuel and/or lube base oil range via Fischer-Tropsch synthesis, comprising:

MANUFACTURE OF FLUID CATALYST

... 1,212,563. Cracking catalysts. MOBIL OIL CORP. 26 April, 1968 [28 April, 1967], No. 19959/68. Heading B1E. [Also in Division C5] A method of preparing a composite fluid catalyst comprises forming a SiO 2 -Al 2 O 3 gel matrix having a pore volume of 0.5 to 1.2 cc/gm and an average pore diameter of 40 to 250Š by precipitating the Al 2 O 3 or SiO 2 gel, dispersing particulate crystalline aluminosilicate zeolite of 2 to 20 micron size and a sodium content of less than 4% in the matrix to form a composite such that the zeolite forms 1-80% of the whole and drying the composite in the form of small particles of a size suitable for use in fluid catalytic cracking, the method being further characterised by admixing with the matrix, prior to dispersal therein of zeolite, a source of zirconia in such amount that there is deposited in the matrix 0.1 to 10% ZrO 2 . Additionally the catalyst may contain rare earth metal cations, Ca++, Mg++ or Mu++.

COMPOSITE CATALYST AND METHOD FOR PREPARING SAME

... 1,218,080. Hydrocarbon conversion catalysts. MOBIL OIL CORP. 29 March, 1968 [31 March, 1967; 26 Dec., 1967], No. 15235/68. Heading D1E. A matrix for the incorporation of an active catalytic component comprises 20-95 % of SiO 2 gel or SiO 2 -ZrO 2 gel and from 5-80% of a "weighting agent", the gel being characterised by a pore volume of at least 0.6 cc./gm. and an alpha () value of less than 0.1 "Weighting agent" is defined as a particulate material denser than SiO 2 or SiO 2 -ZrO 2 gel and non reactive therewith at the temperatures contemplated for preparation and use in hydrocarbon conversion processes. Alpha () is a measure of catalyst activity as set forth in 'Journal of Catalysis', Vol. 4, No. 4 (August 1965) at pp. 525-529. Specified weighting agents are clay, -Al 2 O 3 , zircon, mullite, Al 2 O 3 .H 2 O, Al 2 O 3 .3H 2 O, halloysite, sand, TiO 2 , Si, Al, and Ti. The matrix may support Mo, Co, Cr, W, Fe, Ni, the Pt group metals or oxides and sulphides thereof. Rare earth loaded zeolites ...

SELECTIVE OSOMERIZATION OF 1-OLEFINS TO 2-OLEFINS

... 1346022 Isomerisatioa catalysts AKZONA Inc 16 Feb 1972 [1 March 1971] 7099/72 Heading B1E [Also in Division C5] A catalyst for isomerization of 1-olefins comprises calcium-metal-alumino silicate coated with a monoatomic layer of sodium, and is prepared by stirring and heating the molecular sieve under nitrogen to 200‹C, adding sodium: metal and allowing the mixture to cool under continuous vigorous stirring.

Process for preparing zeolites

Synthetic zeolites are prepared by treating firm calcined non-zeolite particles of fixed size and shape which have been prepared synthetically so as to comprise at least one of the oxides silica and alumina with an aqueous solution containing alkali metal cations and hydroxyl, silicate and aluminate anions, and recovering alkali metal zeolite particles from the solution. The non-zeolite particles may be spheroidal in shape and the process may comprise treating silica with alkali metal aluminate, alumina with alkali metal silicate or alumina and silica with alkali metal hydroxide. The alkali metal may be sodium, potassium or lithium and the proportions in the reaction mixture may be adjusted to give a type A or type X sieve. The alkali metal zeolites may be subjected to ion exchange to give alkaline earth metal zeolites. The non-zeolite particles are calcined at 350-700 DEG C., the temperature of the aqueous treating solution may be 25-150 DEG C. and its pH greater than 11. The silica or ...

Physically stable alumino-silicate zeolite catalysts

An aluminosilicate zeolite is stabilized by calcining at 350-1200 DEG F. in air or an inert gas, e.g. H2 or He, containing >10-50% water. The zeolite may be natural, e.g. fanjasite or mordenite, or synthetic, of formula 0.7-1.1 M2/nO.Al2O3.2.2-14 SiO2, where M is alkali metal; NH4, CO, Ni, Zn, Mg, Ca, Cd, Cu, or Ba (obtained by ion-exchange of the Na form); or H (obtained by calcining the NH4 form). It may, after the calcination, be impregnated with a Pt group metal, e.g. Pd; Co, Fe, Ni, Cu, Ag, Au, Mo, W, V, Zr, Ca, Mg, Hg, Pb or a rare earth metal, or compound thereof. The preparation of 13<\>rA fanjasite from NaOG, Na aluminate, and SiO2 sol is described (Example 1) which was exchanged with a solution of NH4Cl and NH4(OH) (Example 2), dried, and calcined for 16 hours at 650 DEG F. and 2 hours at 950 DEG F. in air containing 16% water (Example 4).

Method for manufacturing catalyst

A method for manufacturing a catalyst, which comprises regenerating a catalyst comprising a zeolite as an active ingredient and having an ethylene conversion lowered through reaction of producing propylene by bringing into contact with ethylene in a vapor phase, by bringing the catalyst into contact with a gas which does not comprise oxygen and comprises hydrogen having a hydrogen partial pressure of 0.01 MPa or more as an absolute pressure thereof.

Modified Zeolite Catalyst Useful for the Conversion of Paraffins, Olefins and Aromatics in a Mixed Feedstock into Isoparaffins and a Process Thereof

The invention relates to a modified zeolite catalyst, useful for the conversion of paraffins, olefins and aromatics in a mixed feedstock such as FCC gasoline that contain high content of olefin, aromatic and n-paraffin into isoparaffins. The invention further relates to the use of such a catalyst, for example but not limited to, in a process for the conversion of paraffins, olefins and aromatics in a mixed feedstock into the product having high amount of branched paraffins with decreased aromatics and olefins, a useful gasoline blend, with negligible production of lighter gases. 14.-. (canceled)5. A process for the preparation of modified zeolite catalyst useful for the conversion of paraffins , olefins and aromatics in a mixed feedstock into isoparaffins , comprising:a) treating the zeolite mordenite with steam, at a temperature of 300-700° C., for 2-6 hours in a shallow bed reactor for dealumination, followed by washing with 0.01-2N acid solution at 100-110° C. for 2-6 hours and further washing with deionized water to remove the extra-framework debris of the zeolite and the nitrate ions;b) shaping the zeolite catalyst obtained in step (a) by mixing it with an inert alumina binder, with zeolite to binder ratio in the range of 3:1 to 3:2.5 by weight, followed by adding 2-3 vol % glacial acetic acid and allowing the above said mixture for peptization to obtain a homogeneous paste, followed by extrusion, drying at 20-30° C., for 10-12 hours and calcinations at 500° C. for 2-6 hours; andc) loading the extruded catalyst obtained in step (b) with the noble metal ions by incipient wet impregnation method (IWI) using Pt tetrammonium chloride and/or Pd chloride as a source of salts, followed by calcination at 500-600° C. for 4-6 hours to obtain the desired modified catalyst.6. The process of claim 5 , wherein the inert alumina binder used in step (b) is pseudo boehmite.7. The process of claim 5 , wherein the steaming temperature used in step (a) is in the range of 350-650° ...

MULTIFUNCTIONAL CATALYST ADDITIVE COMPOSITION AND PROCESS OF PREPARATION THEREOF

The present invention relates to a multifunctional catalyst additive composition for reduction of carbon monoxide and nitrogen oxides in a fluid catalytic cracking process comprising an inorganic oxide; alumino silicate or a zeolite; a noble metal; a metal of Group I A; a metal of Group II A; a metal of Group III A; a metal of Group IV A; a metal of Group V A; a rare earth oxide; at least a metal of Group VIII. The composition is attrition resistant and is incorporated on a support. The present invention also discloses a process for preparing the multifunctional catalyst additive composition. The present invention also discloses a fluid cracking catalyst comprising the multifunctional catalyst additive composition. 1. A multifunctional catalyst additive composition for reduction of carbon monoxide and nitrogen oxides in a fluid catalytic cracking process comprising:(i) an inorganic oxide material.(ii) at least 1% of alumino silicate or a zeolite;(iii) at least 0.001% by weight of a noble metal;(iv) at least 0.01% by weight of a metal of Group I A;(v) at least 0.01% by weight of a metal of Group II A;(vi) at least 0.45% by weight of a metal of Group III A;(vii) at least 0.3% by weight of an element of Group IV A;(viii) at least 0.01% by weight of at least a metal of Group V A;(ix) at least 0.05% by weight of a rare earth oxide;(x) at least 0.02% by weight of at least a metal of Group VIII;wherein said multifunctional additive composition is deposited on to a support and is attrition resistant.2. The multifunctional catalyst additive composition as claimed in wherein said support is a fresh support or discarded refinery catalyst from a cracking petroleum process.3. The multifunctional catalyst additive composition as claimed in wherein said fresh support comprises inorganic oxide or zeoilite with unimodal pore distribution having pores in the range of 20° A to 300° A claim 1 , preferably in the range of 20 to 100° A claim 1 , more preferably in the range of 20 to 60° ...

TITANIA-BOUND ZSM-12 ZEOLITE COMPOSITION AND METHOD OF MAKING AND USING SUCH COMPOSITION

Presented is a composition useful in the catalytic dewaxing of a waxy hydrocarbon feedstock. The composition includes a mixture of ZSM-12 zeolite and titania and may further include a noble metal. The ZSM-12 zeolite preferably has a high silica-to-alumina ratio within its framework. The mixture may be dealuminated either by acid leaching using a fluorosilicate salt or by steam treating. 1. A composition , comprising: a mixture comprising ZSM-12 zeolite and titania.2. A composition as recited in claim 1 , wherein said ZSM-12 zeolite is present in said composition in an amount of at most 70% wt and said titania is present in said composition in an amount of no more than 90% wt claim 1 , with such % wt being based on the dry weight of said composition.3. A composition as recited in claim 2 , further comprising: a noble metal selected from the group of noble metals consisting of platinum and palladium.4. A composition as recited in claim 3 , wherein said mixture is treated with an acid solution to thereby provide dealuminated ZSM-12 zeolite.5. A composition as recited in claim 4 , wherein said dealuminated ZSM-12 zeolite has a silica-to-alumina ratio of at least 50.6. A composition as recited in claim 1 , wherein said ZSM-12 zeolite is dealuminated ZSM-12 zeolite.7. A composition as recited in claim 1 , wherein said ZSM-12 zeolite has a silica-to-alumina molar ratio of at least 50.8. A composition as recited in claim 1 , wherein said mixture is substantially free of silica other than the silica contained in the ZSM-12 zeolite framework.9. A composition as recited in claim 1 , wherein said mixture is substantially free of alumina other than the alumina contained in the ZSM-12 zeolite framework.10. A composition as recited in claim 1 , wherein said titania has a substantial absence of silica.11. A composition as recited in claim 1 , wherein said titania has a substantial absence of alumina.12. A composition as recited in claim 1 , wherein said titania has a surface area ...

Enhanced aromatics production by low pressure end point reduction and selective hydrogenation and hydrodealkylation

A reforming process includes an endpoint reduction zone for converting C 11+ components via selective hydrogenation and hydrodealkylation to lower boiling point aromatics, such as benzene, toluene, and xylene, or their single ring aromatic C 9 -C 10 precursors.

Method for Producing a Platinum Catalyst Precursor

The present invention relates to a method for producing a precursor of a supported platinum catalyst. To provide a method for producing a platinum catalyst precursor, by means of which supported platinum catalysts can be produced which have a relatively high activity, a method is proposed, comprising the steps of: a) impregnating an open-pored support material with platinum sulphite acid; b) calcining the impregnated zeolite material under a protective gas.

Method for producing tertiary amine

The present invention discloses the method for producing a tertiary amine, using the column reactor packed with catalyst layers, containing supplying a liquid and a gaseous raw materials from the bottom of the column, reacting these raw materials in the column, and discharging the product from the top of the column, wherein the column reactor includes two or more honeycomb catalyst layers as the catalyst layers, one or more spaces between each honeycomb catalyst layer, and one or more rectifying sections that prevents a partial or whole back flow of the raw materials, arranged in each space without contacting with the honeycomb catalyst layer.

CATALYSTS FOR IMPROVED CUMENE PRODUCTION AND METHOD OF MAKING AND USING SAME

An aromatic alkylation catalyst is presented. The aromatic alkylation catalyst comprised a zeolite, an inorganic oxide, and silanol functional groups of less than about 0.65 area/mg on the surface of the catalyst. 1. An aromatic alkylation catalyst , comprising:a zeolite;an inorganic oxide; andsilanol functional groups of less than about 0.65 area/mg on a surface of said alkylation catalyst.2. The aromatic alkylation catalyst of claim 1 , wherein said inorganic oxide is selected from the group consisting of silica claim 1 , alumina claim 1 , magnesia claim 1 , zirconia claim 1 , and combinations thereof.3. The aromatic alkylation catalyst of claim 1 , wherein said zeolite has a Si/Almolar ratio between about 18 to about 30.4. The aromatic alkylation catalyst of claim 1 , prepared by the steps of:providing a zeolite;washing said zeolite with water;forming an extrudate from said zeolite and an inorganic oxide;heating said extrudate in a first calcining step to produce a calcined catalyst;exposing the calcined catalyst to an ion exchange solution comprising ammonium ions to produce an ion exchanged catalyst; andheating the ion exchanged catalyst in a second calcining step to produce an alkylation catalyst.5. The aromatic alkylation catalyst of claim 4 , wherein said heating said extrudate comprises a temperature of between about 300° C. to about 650° C. for between about 10 minutes to about 20 hours.6. The aromatic alkylation catalyst of claim 5 , wherein said heating said ion exchange catalyst comprises a temperature of between about 300° C. to about 650° C. for between about 10 minutes to about 20 hours.7. The aromatic alkylation catalyst of claim 6 , wherein said inorganic oxide is selected from the group consisting of silica claim 6 , alumina claim 6 , magnesia claim 6 , zirconia claim 6 , and combinations thereof.8. The aromatic alkylation catalyst of claim 7 , wherein said zeolite has a Si/Almolar ratio between about 18 to about 30.9. A method of preparing an ...

METHODS OF RECOVERING RARE EARTH ELEMENTS

Processes described include reacting a fresh or spent catalyst, or sorbent, with a solution containing an extracting agent (such as an acid or a base). Preferably, the catalyst contains both alumina and a molecular sieve (or a sorbent), and the reaction is performed under relatively mild conditions such that the majority of the base material does not dissolve into the solution. Thus, the catalyst can be re-used, and in certain instances the catalyst performance even improves, with or without re-incorporating certain of the metals back into the catalyst. Additionally, metals contained in the catalyst, such as Na, Mg, Al, P, S, Cl, K, Ca, V, Fe, Ni, Cu, Zn, Sr, Zn Sb, Ba, La, Ce, Pr, Nd, Pb, or their equivalent oxides, can be removed from the catalyst. Some of the metals that are removed are relatively valuable (such as the rare earth elements of La, Ce, Pr and Nd). 1. A method of increasing an amount of zeolite contained in a zeolite-containing material , the method comprising:providing a sample of a zeolite-containing material having at least one rare earth element therein;increasing the amount of zeolite in the sample of the zeolite-containing material by reacting the sample of the zeolite-containing material with an extracting agent that extracts at least a portion of the at least one rare earth element from the sample of the zeolite-containing material;separating the reacted sample, from which has been extracted at least some of the at least one rare earth element previously associated therewith, from the extracting agent; andobtaining the reacted sample in which the percentage increase in the amount of zeolite in the reacted sample is at least 20%.2. The method according to claim 1 , further comprising:repeating the increasing step for multiple iterations, designated as (n) iterations where (n) is a whole number, with an extracting agent that includes at least some of the rare earth element; andrepeating the separating step for (n) iterations.3. The method ...

CATALYSTS AND METHODS FOR PRODUCING ACETIC ACID FROM METHANE, CARBON MONOXIDE, AND OXYGEN

Catalysts for producing one or more oxygenated products from methane are provided. In embodiments, the catalyst comprises active sites comprising isolated, cationic transition metal M′ atoms covalently bound to internal surfaces of pores of a porous metal M″ silicate, wherein M′ is Rh or Ir, and further wherein the M′ atoms are bound to five oxygen (O) atoms. Methods for making and using the catalysts are also provided. 1. A catalyst for producing one or more oxygenated products from methane , the catalyst comprising active sites comprising isolated , cationic transition metal M′ atoms covalently bound to internal surfaces of pores of a porous metal M″ silicate ,wherein M′ is Rh or Ir, andfurther wherein the M′ atoms are bound to five oxygen (O) atoms.2. The catalyst of claim 1 , wherein the active sites have formula (O)=M′≡(O) claim 1 , wherein Ois molecular oxygen and the remaining O atoms are also covalently bound within the porous metal M″ silicate.3. The catalyst of claim 2 , wherein one claim 2 , two claim 2 , or all three of the oxygens of the M′≡(O)bonds are also covalently bound to the M″ of the porous metal M″ silicate claim 2 , thereby providing one claim 2 , two claim 2 , or three M′-O-M″ linkages.4. The catalyst of claim 1 , wherein an external surface of the porous metal M″ silicate is free of M′ atoms claim 1 , the porous metal M″ silicate is free of M′-M′ bonds claim 1 , the porous metal M″ silicate is free of M′ oxide particles claim 1 , or combinations thereof.5. The catalyst of having an amount of M′ in a range of from 0.01 wt % to 0.5 wt %.6. The catalyst of claim 1 , wherein the porous metal M″ silicate is a microporous aluminosilicate.7. The catalyst of claim 6 , wherein the microporous aluminosilicate is a zeolite.8. The catalyst of claim 7 , wherein the zeolite is ZSM-5.9. A catalyst for producing one or more oxygenated products from methane claim 7 , the catalyst comprising active sites comprising isolated claim 7 , cationic transition metal ...

A METHOD FOR PRODUCING A CRYSTALLINE FILM OF ZEOLITE AND/OR ZEOLITE LIKE CRYSTALS ON A POROUS SUBSTRATE

The invention concerns a method for producing a crystalline film comprising zeolite crystals and/or zeolite-like crystals on a porous substrate The method includes the steps of: a) providing a porous substrate, b) rendering at least a part of said porous substrate hydrophobic by treatment with a composition comprising one or more hydrophobic agent(s), d) subjecting said treated porous substrate to a composition comprising zeolite crystals and/or zeolite-like crystals thereby depositing and attaching zeolite crystals and/or zeolite-like crystals on said treated porous substrate, and e) growing a crystalline film comprising zeolite crystals and/or zeolite-like crystals on said treated porous substrate obtained in step d). Crystalline films find use in a variety of fields such as in the production of membranes, catalysts etc. 117.-. (canceled)18. A method for producing a crystalline film comprising zeolite crystals and/or zeolite-like crystals on a porous substrate , said method comprising the steps of:a) providing a porous substrate comprising pores,b) masking at least a portion of said porous substrate by treatment with a composition comprising one or more hydrophobic agent(s), thereby providing a hydrophobic porous substrate surface,d) subjecting said hydrophobic porous substrate surface to a composition comprising seed zeolite crystals and/or seed zeolite-like crystals thereby depositing said seed zeolite crystals and/or seed zeolite-like crystals on said hydrophobic porous substrate surface, ande) growing a crystalline film comprising zeolite crystals and/or zeolite-like crystals on said hydrophobic porous substrate surface obtained in step d), thereby producing a crystalline film comprising zeolite crystals and/or zeolite-like crystals on the porous substrate, wherein said hydrophobic porous substrate surface substantially prevents the crystalline film comprising zeolite crystals and/or zeolite-like crystals from depositing in the pores of said hydrophobic porous ...

MESOPOROUS ZEOLITES AND METHODS FOR THE SYNTHESIS THEREOF

Methods for producing mesoporous zeolites are provided. In some embodiments, the method includes mixing a silicon-containing material, an aluminum-containing material, or both, with a quaternary amine and at least one base to produce a zeolite precursor solution. The zeolite precursor solution is combined with nanocellulose to form a zeolite precursor gel, from which volatiles are removed. The zeolite precursor gel is crystallized to produce a crystalline zeolite intermediate. The crystalline zeolite intermediate is calcined to form the mesoporous zeolite. The nanocellulose mesopores template may include cellulose nanocrystals, nanocellulose fibers, or combinations thereof. The quaternary amine may include tetraethylammonium hydroxide, tetraethylamonnium alkoxide, tetrapropylammonium alkoxide, other alkaline materials comprising ammonium, or combinations thereof. 1. A method for producing a mesoporous zeolite , the method comprising:mixing a silicon-containing material, an aluminum-containing material, or both, with at least a quaternary amine and at least one base to produce a zeolite precursor solution;combining a nanocellulose mesopore template with the zeolite precursor solution to produce a zeolite precursor gel;crystallizing the zeolite precursor gel to produce a crystalline zeolite intermediate; andcalcining the crystalline zeolite intermediate to produce the mesoporous zeolite.2. The method of claim 1 , further comprising removing at least a solvent from the precursor gel prior to the crystallizing.3. The method of claim 1 , wherein the crystallization comprises contacting the zeolite precursor gel with steam.4. The method of claim 1 , wherein the crystalline zeolite intermediate is calcined by exposure to a temperature of at least 500° C.5. The method of claim 1 , wherein the nanocellulose mesopore template comprises at least one of cellulose nanocrystals claim 1 , nanocellulose fibers claim 1 , or combinations thereof.6. The method of claim 1 , wherein the ...

METHOD FOR PRODUCING C4-C15 LACTAMS

The present invention relates to a process for preparing C-Clactams, in which a C-C-alkyl nitrite is reacted with a C-C-cycloalkane and is illuminated with a light-emitting diode during the reaction. This forms a C-C-cyclohexanone oxime which is then converted further to a C-Clactam; the C-Calcohol formed is recycled into the preparation of the C-C-alkyl nitrite. 112.-. (canceled)13. A process for preparing C-Clactams , comprising the steps of:{'sub': 1', '10', '1', '10, 'a) converting a first mixture (M1) comprising a C-Calcohol, nitrogen oxides and oxygen to obtain a C-C-alkyl nitrite,'}{'sub': 1', '10', '4', '15', '4', '15', '4', '15', '4', '15', '1', '10, 'claim-text': 'wherein the second mixture (M2) is illuminated during the conversion with a light-emitting diode that emits light having a wavelength in the range from 300 to 500 nm,', 'b) converting a second mixture (M2) comprising the C-C-alkyl nitrite obtained in step a) and a C-C-cycloalkane to obtain a first product mixture (P1) comprising a C-C-nitrosocycloalkane, a dimeric C-C-nitrosocycloalkane, a C-C-cycloalkanone oxime and a C-Calcohol,'}{'sub': 4', '15', '4', '15, 'claim-text': [{'sub': 1', '10', '4', '15, 'claim-text': [{'sub': 1', '10, 'recycling the C-Calcohol removed into the first mixture (M1) in step a) and'}, {'sub': 4', '15', '4', '15, 'converting the C-C-cycloalkanone oxime present in the second product mixture (P2) in the presence of the catalyst to obtain the C-Clactam,'}], 'c1) separating the C-Calcohol from the first product mixture (P1) obtained in step b) to obtain a second product mixture (P2) comprising the C-C-cycloalkanone oxime,'}, 'or', {'sub': 1', '15', '4', '15', '1', '10, 'claim-text': [{'sub': 1', '10', '1', '15, 'removing the C-Calcohol present in the third product mixture (P3) to obtain the C-Clactam and'}, {'sub': 1', '10, 'recycling the C-Calcohol removed into the first mixture (M1) in step a).'}], 'c2) converting the C-C-cycloalkanone oxime present in the first product ...

ZONE COATED CATALYTIC SUBSTRATES WITH PASSIVE NOX ADSORPTION ZONES

Disclosed are methods of forming zone coated substrates for use in catalytic converters, as well as washcoat compositions and methods suitable for using in preparation of the zone coated substrates, and the zone coated substrates formed thereby. The zone coated substrates can include a Passive NOAdsorption zone and a catalytic zone. Also disclosed are exhaust treatment systems, and vehicles, such as diesel vehicles, using catalytic converters and exhaust treatment systems using the zone coated substrates. 1. A coated substrate comprising: the first zone comprising a Passive NOx Adsorber (PNA) layer comprising nano-sized platinum group metal (PGM) on a plurality of support particles comprising cerium oxide; and', 'the second zone comprising a first catalytic layer comprising a first composite nanoparticle, wherein the first composite nanoparticle comprises a first catalytic nanoparticle on a first support nanoparticle., 'a substrate comprising a first zone and a second zone;'}2. The coated substrate of claim 1 , wherein the first composite nanoparticle is plasma created.3. (canceled)4. The coated substrate of claim 1 , wherein the first composite nanoparticle is bonded to a micron-sized carrier particle to form a first NNm particle.5. The coated substrate of claim 1 , wherein the first composite nanoparticle is embedded within carrier particles to form a first NNiM particle.6. The coated substrate of claim 1 , wherein the second zone further comprises a second catalytic layer comprising a second composite nanoparticle claim 1 , wherein the second composite nanoparticle comprises a second catalytic nanoparticle on a second support nanoparticle.78-. (canceled)9. The coated substrate of claim 1 , wherein the first claim 1 , second claim 1 , or first and second catalytic nanoparticles comprise platinum and palladium.1012-. (canceled)13. The coated substrate of claim 1 , wherein the second zone further comprises a zeolite layer comprising zeolite particles.14. The coated ...

ZEOLITIC CATALYTIC CONVERSION OF ALCOHOLS TO OLEFINS

A catalyst composition for converting an alcohol to olefins, the catalyst composition comprising the following components: (a) beta zeolite; (b) at least one element selected from the group consisting of zinc, magnesium, calcium, strontium, sodium, and potassium; and (c) at least one element selected from the group consisting of hafnium, yttrium, zirconium, tantalum, niobium, and tin; wherein the components (b) and (c) are independently within or on a surface of said beta zeolite. The catalyst may also further include component (d), which is copper or silver. Also described herein is a method for converting an alcohol to one or more olefinic compounds, the method comprising contacting the alcohol with a catalyst at a temperature of at least 100° C. and up to 500° C. to result in the alcohol being converted to the one or more olefinic compounds. 1. A catalyst composition for converting an alcohol to olefins , the catalyst composition comprising the following components:(a) beta zeolite;(b) at least one element selected from the group consisting of zinc, magnesium, calcium, strontium, sodium, and potassium; and(c) at least one element selected from the group consisting of hafnium, yttrium, zirconium, tantalum, niobium, and tin;wherein the components (b) and (c) are independently within or on a surface of said beta zeolite.2. The catalyst composition of claim 1 , further comprising component (d) claim 1 , which is copper or silver.3. The catalyst composition of claim 1 , wherein said beta zeolite is dealuminated and has a silicon to aluminum ratio of at least 10.4. The catalyst composition of claim 1 , wherein said component (b) comprises zinc.5. The catalyst composition of claim 1 , wherein said component (c) comprises hafnium or yttrium. The catalyst composition of claim 1 , wherein said component (b) comprises zinc and said component (c) comprises hafnium or yttrium.7. The catalyst composition of claim 2 , wherein at least one of said copper or silver is on a ...

ZEOLITE COATING PREPARATION ASSEMBLY AND OPERATION METHOD

The present invention relates to a zeolite coating preparation assembly and operation method wherein zeolite adsorbents are coated by crystallization process on various surfaces heated by induction. The objective of the present invention is to provide a zeolite coating preparation assembly and operation method; by which time saving is achieved owing to heating by induction, material saving is achieved owing to heating by induction, material saving is achieved since large heating resistances and complicated reactors are not used; and which is thus more economical; and wherein thicker and more stable coatings with high diffusion coefficients are prepared by using a more practical reaction system in a shorter period of time in comparison to the known methods, and wherein mass production is enabled. 1. A zeolite coating preparation method for performing in the assembly , comprising the steps of:preparing a reactor, which is made of a material with low electrical conductivity;preparing a synthesis solution as diluted and filling it into the reactor;cleaning an electrically conductive substrate and placing it in the synthesis solution filled into the reactor;placing the reactor near a coil of an induction device;adjusting the distance between the coil and the reactor and/or the power of the induction device so as to provide the desired substrate temperature;circulating the synthesis solution that is in the reactor by the help of a pump via a connection line lying between a feeding tank which is immersed in a water bath, and the reactor;adjusting the water bath temperature with the help of a heat exchanger in order to keep the temperature of the synthesis solution in the feeding tank at a value to assure that the temperature of the synthesis solution in the reactor remains at a desired value that is lower than the temperature of the substrate;producing magnetic field by operating the induction device;performing the synthesis at the desired substrate and solution ...

LOWER-HYDROCARBON AROMATIZATION CATALYST AND METHOD FOR PRODUCING LOWER-HYDROCARBON AROMATIZATION CATALYST

To contribute to the improvement of catalytic activity of a lower hydrocarbon aromatization catalyst, which converts a lower hydrocarbon(s) to an aromatic compound(s), and to the improvement of compactability of the catalyst. 17-. (canceled)8. A lower hydrocarbon aromatization catalyst characterized by being formed by compacting a catalyst-supported , metallosilicate mixture of a first metallosilicate having a catalyst metal supported on a metallosilicate having a Si/Al ratio of 10-100 and a second metallosilicate supporting thereon the catalyst metal , having a Si/Al ratio of 10-100 , and having an average grain size smaller than that of the first metallosilicate.9. The lower hydrocarbon aromatization catalyst according to claim 8 , which is characterized by that the average grain size of the second metallosilicate is one fifth or less of that of the first metallosilicate.10. The lower hydrocarbon aromatization catalyst according to claim 9 , which is characterized by that the average grain size of the first metallosilicate is from 1.0 μm to 5.0 μm.11. The lower hydrocarbon aromatization catalyst according to claim 9 , which is characterized by that the average grain size of the second metallosilicate is from 0.1 μm to 1.0 μm.12. The lower hydrocarbon aromatization catalyst according to claim 8 , which is characterized by that the second metallosilicate is added by from 20% to 80% claim 8 , relative to mass of the mixture.13. A process for producing a lower hydrocarbon aromatization catalyst for converting a lower hydrocarbon to an aromatic compound and is characterized bythat a first metallosilicate having a Si/Al ratio of 10-100, on which a catalyst metal is to be supported, and a second metallosilicate having an average grain size smaller than that of the first metallosilicate and having a Si/Al ratio of 10-100 are mixed together,that the metal catalyst is supported on a mixture obtained by the mixing, andthat this catalyst metal supported mixture is compacted. ...

Low-Temperature Oxidation Catalyst With Particularly Marked Hydrophobic Properties For The Oxidation Of Organic Pollutants

The present invention relates to a catalyst comprising a macroporous noble metal-containing zeolite material and a porous SiO-containing binder, wherein the catalyst has a proportion of micropores of more than 70%, based on the total pore volume of the catalyst. The invention is additionally directed to a process for preparing the catalyst and to the use of the catalyst as an oxidation catalyst. 19.-. (canceled)10. Method of producing a catalyst according to , comprising the following steps:a) introducing a noble metal precursor compound into a microporous zeolite material;b) calcining the zeolite material loaded with the noble metal precursor compound;{'sub': '2', 'c) mixing the zeolite material loaded with the noble metal compound with a porous SiO-containing binder and a solvent;'}d) drying and calcining the mixture comprising the zeolite material loaded with the noble metal compound and the binder.11. Method according to claim 10 , wherein the mixture obtained in step c) is applied to a support.12. (canceled) The present invention relates to a catalyst comprising a microporous noble metal-containing zeolite material and a porous SiO-containing binder, wherein the catalyst has a proportion of micropores of more than 70%, relative to the total pore volume of the catalyst. The invention is additionally directed to a method of producing the catalyst as well as to the use of the catalyst as oxidation catalyst.Purifying exhaust gases by means of catalysts has been known for some time. For example, the exhaust gases from combustion engines are purified with so-called three-way catalysts (TWC). The nitrogen oxides are reduced with reductive hydrocarbons (HC) and carbon monoxide (CO).Likewise, the exhaust gases from diesel engines are post-treated with catalysts. Here, carbon monoxide, unburnt hydrocarbons, nitrogen oxides and soot particles, for example, are removed from the exhaust gas. Unburnt hydrocarbons which are to be treated catalytically include paraffins, ...

Catalyst Support and Process for the Preparation Thereof

An amorphous catalyst support comprising at least a first oxide selected from the group consisting of: silica, germanium oxide, titanium oxide, zirconium oxide or mixtures thereof, preferably silica gel beads or diatomaceous earth; a group 3 metal oxide; and anions in an amount not greater than 10% by weight of the catalyst support; wherein the group 3 metal oxide is incorporated in the first oxide structure at the molecular level. The catalyst support is prepared by (a) mixing the first oxide, with an anhydrous source of the group 3 metal oxide, and water, at a pH above 11, thus forming a suspension, (b) washing the catalyst support with water, (c) separating the catalyst support from the water, and (d) optionally drying and/or calcining the catalyst support. A catalyst based on such a support has improved catalytic properties. 1. A process for the preparation of a catalyst support , the process comprising:(a) mixing silica gel beads or diatomaceous earth with an anhydrous source of alumina and water, at a pH above 11, thus forming a suspension,(b) optionally washing the catalyst support with water,(c) separating the catalyst support from the water,(d) optionally drying and/or calcining the catalyst support.2. A process as claimed in claim 1 , wherein the temperature in step (a) is in the range of from 30 to 90° C.3. The process as claimed in claim 1 , wherein the temperature in step (a) is in the range of from 55 to 85° C.4. The process as claimed in claim 1 , wherein the anhydrous source of alumina comprises a metal-alumina claim 1 , preferably sodium aluminate.5. The process as claimed in claim 2 , wherein the anhydrous source of alumina comprises a metal-alumina claim 2 , preferably sodium aluminate.6. The process as claimed in claim 1 , wherein the mixture in step (a) is stirred for from 5 to 90 minutes.7. The process as claimed in claim 1 , wherein the mixture in step (a) is stirred for from 15 to 60 minutes.8. The process as claimed in claim 1 , wherein the ...

EXHAUST GAS PURIFICATION CATALYST AND PRODUCTION METHOD THEREOF

This catalyst includes a lower catalytic layer having catalytic ability to oxidize HC and CO and an upper catalytic layer having catalytic ability to reduce NO. The lower catalytic layer contains Pt and Pd acting as catalytic metals, zeolite, a Ce-containing oxide, and activated alumina, and the upper catalytic layer contains activated alumina loading an Rh-doped Ce-containing oxide and an NOstorage material. 1. An exhaust gas purification catalyst comprising:a lower catalytic layer having catalytic ability to oxidize HC and CO on a substrate; and{'sub': 'x', 'an upper catalytic layer having catalytic ability to reduce NOon top of, or above, the lower catalytic layer, wherein'}the lower catalytic layer contains Pt and Pd acting as catalytic metals, zeolite, Ce-containing oxide, and activated alumina, and{'sub': 'x', 'the upper catalytic layer contains activated alumina loading an Rh-doped Ce-containing oxide and an NOstorage material.'}2. The exhaust gas purification catalyst of claim 1 , whereinthe lower catalytic layer includes a first oxidation catalyst layer containing activated alumina loading Pt and Pd and a Ce-containing oxide loading Pt and Pd, and a second oxidation catalyst layer containing zeolite loading Pt and Pd, andthe second oxidation catalyst layer is disposed on the first oxidation catalyst layer.3. The exhaust gas purification catalyst of claim 1 , wherein{'sub': 'x', 'an intermediate catalytic layer is provided between the lower and upper catalytic layers, the intermediate catalytic layer containing Pt and Rh acting as catalytic metals, activated alumina, a Ce-containing oxide and an NOstorage material, and containing no Pd.'}4. The exhaust gas purification catalyst of claim 2 , wherein{'sub': 'x', 'an intermediate catalytic layer is provided between the lower and upper catalytic layers, the intermediate catalytic layer containing Pt and Rh acting as catalytic metals, activated alumina, a Ce-containing oxide and an NOstorage material, and ...

GD-CONTAINING, ANTI-COKING SOLID ACID CATALYSTS AND PREPARATION METHOD AND USE THEREOF

The present invention relates to an anti-coking catalyst having a physical property of reducing coke formation, which comprises a solid acid catalyst containing gadolinium (Gd) on the surface, a preparation method thereof, and a use thereof. The preparation method includes a first step of determining the amount of gadolinium (Gd) or a Gd-providing precursor to be used relative to the total weight of the solid acid catalyst, which reduces the coking of a specific solid acid catalyst below a specific level under a specific reaction condition; and a second step of preparing a Gd-containing solid acid catalyst using the amount determined in the first step. 1. A method of preparing an anti-coking solid acid catalyst having a physical property of reducing coke formation , comprising:a first step of determining the amount of gadolinium (Gd) or Gd-providing precursor to be used relative to the total weight of the solid acid catalyst, which reduces the coking of a specific solid acid catalyst below a specific level under a specific reaction condition in which the catalyst is intended to be used; anda second step of preparing a Gd-containing solid acid catalyst using the amount determined in the first step.2. The method according to claim 1 , wherein the Gd-containing solid acid catalyst prepared in the second step has an increased number of a base site of the solid acid catalyst by the presence of gadolinium.3. The method according to claim 1 , wherein the Gd-containing solid acid catalyst prepared in the second step has a film containing Gd metal or gadolinium oxide formed on the surface of the solid acid catalyst with a nano-size thickness.4. The method according to claim 1 , wherein the amount of gadolinium to be used relative to the total weight of the solid acid catalyst is determined from the temperature-programmed desorption curve of carbon dioxide claim 1 , base strength claim 1 , or base site density per gadolinium content.5. The method according to claim 1 , ...

Acidic Aromatization Catalyst with Improved Activity and Stability

Methods for producing supported catalysts containing a transition metal and a bound zeolite base are disclosed. These methods employ a step of impregnating the bound zeolite base with the transition metal, fluorine, and high loadings of chlorine. The resultant high chlorine content supported catalysts have improved catalyst activity in aromatization reactions. 1. A supported catalyst comprising:a bound zeolite base;from about 0.3 wt. % to about 3 wt. % of a transition metal;from about 1.8 wt. % to about 4 wt. % of chlorine; andfrom about 0.4 wt. % to about 1.5 wt. % of fluorine, based on the total weight of the supported catalyst;wherein the supported catalyst is characterized by a peak reduction temperature on a Temperature Programmed Reduction curve in a range from about 580° F. to about 800° F.2. The catalyst of claim 1 , wherein the bound zeolite base comprises from about 5 wt. % to about 30 wt. % of a binder claim 1 , based on the total weight of the bound zeolite base.3. The catalyst of claim 1 , wherein:the bound zeolite base comprises a silica-bound K/L-zeolite;the transition metal comprises platinum; anda weight ratio of chlorine:fluorine is in a range from about 2:1 to about 5:1.4. The catalyst of claim 1 , wherein the supported catalyst comprises:from about 0.5 wt. % to about 2 wt. % of platinum;from about 2.2 wt. % to about 3.4 wt. % of chlorine; andfrom about 0.5 wt. % to about 1.1 wt. % of fluorine.5. The catalyst of claim 4 , wherein the supported catalyst is characterized by a peak reduction temperature on a Temperature Programmed Reduction curve in a range from about 600° F. to about 720° F.6. The catalyst of claim 1 , wherein the supported catalyst has a total nitrogen content that is greater than that of a catalyst having from 0.3 wt. % to 1.5 wt. % chlorine claim 1 , under the same catalyst preparation conditions.7. The catalyst of claim 1 , wherein the supported catalyst is characterized by a Temperature Programmed Reduction curve comprising a ...

CATALYTIC HYDROCARBON DEHYDROGENATION

A catalyst for dehydrogenation of hydrocarbons includes a support including zirconium oxide and Linde type L zeolite (L-zeolite). A concentration of the zirconium oxide in the catalyst is in a range of from 0.1 weight percent (wt. %) to 20 wt. %. The catalyst includes from 5 wt. % to 15 wt. % of an alkali metal or alkaline earth metal. The catalyst includes from 0.1 wt. % to 10 wt. % of tin. The catalyst includes from 0.1 wt. % to 8 wt. % of a platinum group metal. The alkali metal or alkaline earth metal, tin, and platinum group metal are disposed on the support. 1. A catalyst for dehydrogenation of hydrocarbons , the catalyst comprising:a support comprising zirconium oxide and Linde type L zeolite (L-zeolite), wherein a concentration of the zirconium oxide in the catalyst is in a range of from 0.1 weight percent (wt. %) to 20 wt. %;from 5 wt. % to 15 wt. % of an alkali metal or alkaline earth metal, the alkali metal or alkaline earth metal disposed on the support;from 0.1 wt. % to 10 wt. % of tin, the tin disposed on the support; andfrom 0.1 wt. % to 8 wt. % of a platinum group metal, the platinum group metal disposed on the support.2. The catalyst of claim 1 , wherein the alkali metal or alkaline earth metal is selected from the group consisting of lithium claim 1 , sodium claim 1 , potassium claim 1 , rubidium claim 1 , cesium claim 1 , beryllium claim 1 , magnesium claim 1 , calcium claim 1 , and barium.3. The catalyst of claim 2 , wherein the alkali metal is potassium or cesium.4. The catalyst of claim 2 , wherein the platinum group metal is selected from the group consisting of platinum claim 2 , ruthenium claim 2 , iridium claim 2 , rhodium claim 2 , and palladium.5. The catalyst of claim 2 , wherein the catalyst is configured to dehydrogenate hydrocarbons including 3 to 6 carbon atoms at an operating temperature in a range of from about 500 degrees Celsius (° C.) to about 800° C. and an operating pressure in a range of from about 0.01 bar to about 10 bar.6. ...

A Process For Preparing A Catalyst

The present disclosure relates to a process for preparing a catalyst. The process comprises coating zeolite gel over the alumina support to obtain a chloride free zeolite gel coated alumina support, crystallizing the chloride free zeolite gel coated alumina support, washing, drying and calcining the crystallized zeolite coated alumina support to obtain a calcined crystallized chloride free zeolite coated alumina support, treating the calcined crystallized chloride free zeolite coated alumina support with ammonium nitrate to obtain sodium free support, washing, drying, and calcining the support to obtain a calcined chloride free zeolite coated alumina support, immersing the calcined chloride free zeolite coated alumina support in an active metal and a promoter metal solution mixture followed by stirring to obtain a metal coated chloride free zeolite coated alumina support, and drying and calcining the metal coated chloride free zeolite coated alumina support to obtain the catalyst. 1. A process for preparing a catalyst comprising the following steps:a) providing alumina support;b) coating zeolite gel over the alumina support to obtain a chloride free zeolite gel coated alumina support;c) crystallizing the chloride free zeolite gel coated alumina support to obtain a crystallized zeolite coated alumina support;d) washing, drying and calcining the crystallized chloride free zeolite coated alumina support to obtain a calcined crystallized chloride free zeolite coated alumina support;e) treating the calcined crystallized chloride free zeolite coated alumina support with ammonium nitrate to obtain sodium free support; andf) washing, drying, and calcining the support to obtain a calcined chloride free zeolite coated alumina support.g) immersing the calcined chloride free zeolite coated alumina support in an active metal and a promoter metal solution mixture followed by stirring to obtain a metal coated chloride free zeolite coated alumina support; andh) drying and calcining ...

Catalyst For A Naphtha Reforming Process

The present disclosure relates to a catalyst for a naphtha reforming process. The catalyst comprises a chloride free zeolite coated alumina support impregnated with 0.01 wt % to 0.5 wt % active metal and 0.01 wt % to 0.5 wt % promoter metal, characterized in that the thickness of the zeolite coating on the alumina support ranges from 100 μm to 200 μm. 1. A catalyst comprising a chloride free zeolite coated alumina support impregnated with 0.01 wt % to 0.5 wt % active metal and 0.01 wt % to 0.5 wt % promoter metal , wherein the thickness of said zeolite coating on said chloride free alumina support ranges from 100 μm to 200 μm.2. The catalyst as claimed in claim 1 , wherein said zeolite is at least one selected from a group consisting of ZSM-5 claim 1 , mordenite claim 1 , USY claim 1 , H-Beta claim 1 , MCM-22 claim 1 , and ZSM-12.3. The catalyst as claimed in claim 1 , wherein said zeolite is ZSM-5 comprising SiOand AlO.4. The catalyst as claimed in claim 3 , wherein said zeolite is ZSM-5 having the ratio of SiOto AlOranging from 10:1 to 20:1 claim 3 , preferably 15:1.5. The catalyst as claimed in claim 1 , wherein said active metal is at least one selected from the group consisting of platinum (Pt) claim 1 , palladium (Pd) and nickel (Ni).6. The catalyst as claimed in claim 1 , wherein said active metal is platinum (Pt).7. The catalyst as claimed in claim 1 , wherein said promoter metal is at least one selected from the group consisting of tin (Sn) claim 1 , rhenium (Re) and Iridium (Ir).8. The catalyst as claimed in claim 1 , wherein said promoter metal is tin (Sn). The present disclosure relates to a catalyst for a naphtha reforming process.An active metal is a Group VIII metal of the modern periodic table. The Group VIII metals are platinum (Pt), palladium (Pd) and nickel (Ni).A promoter metal is a Group IV metal of the modern periodic table. The Group IV metals are tin (Sn), rhenium (Re) and iridium (Ir).ZSM-5 is an aluminosilicate zeolite belonging to the ...

PLATINUM GROUP METAL (PGM) CATALYST FOR TREATING EXHAUST GAS

Provided are catalysts comprising a small pore molecular sieve embedded with platinum group metal (PGM) and methods for treating lean burn exhaust gas using the same. 1. A catalyst comprising:a. a small pore aluminosilicate molecular sieve material comprising a plurality of crystals having a surface and a porous network; andb. at least one Platinum Group Metal (PGM),wherein a majority amount of said PGM is embedded in said porous network relative to PGM disposed on said surface.2. The catalyst of claim 1 , wherein said aluminosilicate molecular sieve has a silica-to-alumina ratio of about 8 to about 150 and an alkali content of no more than about 5 weight percent based on the total weight of the aluminosilicate molecular sieve.3. The catalyst of claim 2 , wherein said catalyst comprises about 0.01 to about 10 weight percent PGM relative to weight of the molecular sieve.4. The catalyst of claim 2 , wherein said catalyst comprises about 0.1 to about 1 weight percent PGM relative to weight of the molecular sieve.5. The catalyst of claim 2 , wherein the small pore molecular sieve material comprises a plurality of crystals having a mean crystalline size of about 0.01 to about 10 microns.6. The catalyst of claim 2 , wherein the small pore molecular sieve material comprises a plurality of crystals having a mean crystalline size of about 0.5 to about 5 microns.7. The catalyst of claim 5 , wherein the small pore molecular sieve material has a framework selected from ACO claim 5 , AEI claim 5 , AEN claim 5 , AFN claim 5 , AFT claim 5 , AFX claim 5 , ANA claim 5 , APC claim 5 , APD claim 5 , ATT claim 5 , CDO claim 5 , CHA claim 5 , DDR claim 5 , DFT claim 5 , EAB claim 5 , EDI claim 5 , EPI claim 5 , ERI claim 5 , GIS claim 5 , GOO claim 5 , IHW claim 5 , ITE claim 5 , ITW claim 5 , LEV claim 5 , KFI claim 5 , MER claim 5 , MON claim 5 , NSI claim 5 , OWE claim 5 , PAU claim 5 , PHI claim 5 , RHO claim 5 , RTH claim 5 , SAT claim 5 , SAV claim 5 , SIV claim 5 , THO claim 5 , ...

SYSTEM AND METHOD FOR CREATING CATALYST OBD LIMIT PARTS FOR EXHAUST AFTERTREATMENT APPLICATIONS

Catalyst diagnostic limit parts and methods for making catalyst diagnostic limit parts are disclosed. An exemplary catalyst diagnostic limit part includes a substrate and a washcoat coating the substrate. The washcoat includes an active catalyst and an inactive catalyst at a predetermined ratio of active catalyst to inactive catalyst so as to control the performance of the catalyst diagnostic limit part. 1. A catalyst diagnostic limit part , comprising:a substrate; anda washcoat coating the substrate, the washcoat including an active catalyst and an inactive catalyst at a predetermined ratio of active catalyst to inactive catalyst so as to control the performance of the catalyst diagnostic limit part.2. The catalyst diagnostic limit part of claim 1 , wherein the predetermined ratio is no higher than 30%:70%.3. The catalyst diagnostic limit part of claim 1 , wherein the predetermined ratio is no higher than 25%:75%.4. The catalyst diagnostic limit part of claim 1 , wherein the inactive catalyst is prepared by thermal aging an active catalyst.5. The catalyst diagnostic limit part of claim 1 , wherein the inactive catalyst includes a chemically-inert material.6. The catalyst diagnostic limit part of claim 5 , wherein the chemically-inert material includes un-exchanged zeolites.7. The catalyst diagnostic limit part of claim 1 , wherein the substrate has a length to diameter ratio of at least 0.33.8. The catalyst diagnostic limit part of claim 1 , wherein the substrate is fully-coated by the washcoat.9. The catalyst diagnostic limit part of claim 1 , wherein the catalyst diagnostic limit part is a diesel oxidation catalyst.10. The catalyst diagnostic limit part of claim 9 , wherein the washcoat includes a predetermined amount of platinum group metal loading less than a conventionally-full amount claim 9 , the predetermined amount defining the predetermined ratio.11. The catalyst diagnostic limit part of claim 1 , wherein the catalyst diagnostic limit part is one of a ...

MULTICOMPONENT EXHAUST TREATMENT SYSTEM INCLUDING AN OXYGEN STORAGE CATALYST

Methods and systems are provided for a multicomponent aftertreatment device arranged in a vehicle exhaust gas passage. In one example, a system may include an oxygen storage catalyst and an underbody trap catalyst comprising metal modified zeolite, the oxygen storage catalyst arranged upstream of the underbody trap catalyst in an exhaust passage of the vehicle. 1. A system for a vehicle , comprising:an oxygen storage catalyst; andan underbody trap catalyst comprising metal modified zeolite, the oxygen storage catalyst arranged upstream of the underbody trap catalyst in an exhaust passage of the vehicle.2. The system of claim 1 , wherein the oxygen storage catalyst comprises an oxygen storage material loaded on or impregnated in a carrier body claim 1 , the oxygen storage material including nickel claim 1 , iron claim 1 , and/or cerium.3. The system of claim 2 , wherein the carrier body comprises cordierite claim 2 , zirconium oxide claim 2 , silicon carbide claim 2 , or silica gel.4. The system of claim 2 , wherein the oxygen storage material is present in the oxygen storage catalyst at 10% or greater weight per weight of the carrier body.5. The system of claim 1 , wherein the underbody trap catalyst further comprises a three-way catalyst washcoat claim 1 , the three-way catalyst washcoat including one or more platinum group metals claim 1 , and wherein the metal modified zeolite comprises platinum group metal modified zeolite.6. The system of claim 1 , further comprising an engine coupled to the exhaust passage and a three-way catalyst coupled downstream of the engine and upstream of the oxygen storage catalyst in the exhaust passage of the vehicle claim 1 , wherein the three-way catalyst is positioned in the exhaust passage 13-33 cm from the engine claim 1 , and wherein the underbody trap catalyst is positioned in the exhaust passage 25 cm or greater from the three-way catalyst.7. The system of claim 1 , further comprising a controller storing instructions in non- ...

Low-temperature oxidation catalyst with particularly marked hydrophobic properties for the oxidation of organic pullutants

The present invention relates to a catalyst comprising a macroporous noble metal-containing zeolite material and a porous SiO 2 -containing binder, wherein the catalyst has a proportion of micropores of more than 70%, based on the total pore volume of the catalyst. The invention is additionally directed to a process for preparing the catalyst and to the use of the catalyst as an oxidation catalyst.

OXIDATION CATALYST FOR INTERNAL COMBUSTION ENGINE EXHAUST GAS TREATMENT

The invention provides an exhaust gas cleaning oxidation catalyst and in particular to an oxidation catalyst for cleaning the exhaust gas discharged from internal combustion engines of compression ignition type (particularly diesel engines). The invention further relates to a catalysed substrate monolith comprising an oxidising catalyst on a substrate monolith for use in treating exhaust gas emitted from a lean-burn internal combustion engine. In particular, the invention relates to a catalysed substrate monolith comprising a first washcoat coating and a second washcoat coating, wherein the second washcoat coating is disposed in a layer above the first washcoat coating. 1. An oxidation catalyst for the oxidative treatment of a hydrocarbon (HC) and carbon monoxide (CO) in an exhaust gas , the oxidation catalyst comprising a supporting substrate and a plurality of catalyst layers supported on the supporting substrate , wherein the plurality of catalyst layers comprise a washcoat material , an active metal and a hydrocarbon adsorbent , and wherein one catalyst layer lies on a catalyst surface layer side and one or more other catalyst layers lie on a side between the said one catalyst layer and the supporting substrate; and wherein:(a) the amount of hydrocarbon adsorbent in the said one catalyst layer is greater than the amount of hydrocarbon adsorbent in the said one or more other catalyst layers, and the concentration of active metal in the said one catalyst layer is the same as or less than the concentration of active metal in the said one or more other catalyst layers; or(b) the amount of hydrocarbon adsorbent in the said one catalyst layer is the same as the amount of hydrocarbon adsorbent in the said one or more other catalyst layers, and the concentration of active metal in the said one catalyst layer is less than the concentration of active metal in the said one or more other catalyst layers.2. An oxidation catalyst according to claim 1 , wherein the hydrocarbon ...

HYDROCARBON OIL DESULFURIZATION ADSORBING AGENT, PRODUCTION AND USE THEREOF

This disclosure provides an adsorbing agent which, on the basis of the total weight of the adsorbing agent, comprises the following components: 1) a Si—Al molecular sieve having a BEA structure, in an amount of 1-20 wt %, 2) at least one binder selected from the group consisting of titanium dioxide, stannic oxide, zirconium oxide and alumina, in an amount of 3-35 wt %, 3) a silica source, in an amount of 5-40 wt %, 4) zinc oxide, in an amount of 10-80 wt %, and 5) at least one promoter metal selected from the group consisting of cobalt, nickel, iron and manganese, based on the metal, in an amount of 5-30 wt %, wherein at least 10 wt % of the promoter metal is present in a reduced valence state. The adsorbing agent exhibits improved activity and stability, and at the same time, is capable of significantly improving the octane number of the product gasoline. 1. A desulfurization adsorbing agent for hydrocarbon oil , on the basis of the total weight of the adsorbing agent , comprising the following components ,1) a Si—Al molecular sieve having a BEA structure, in an amount of 1-20 wt %,2) at least one binder selected from the group consisting of titanium dioxide, stannic oxide, zirconium oxide and alumina, in an amount of 3-35 wt %,3) a silica source, in an amount of 5-40 wt %,4) zinc oxide, in an amount of 10-80 wt %, and5) at least one promoter metal selected from the group consisting of cobalt, nickel, iron and manganese, based on the metal, in an amount of 5-30 wt %, wherein at least 10 wt % of the promoter metal is present in a reduced valence state.2. The adsorbing agent according to claim 1 , wherein the Si—Al molecular sieve having a BEA structure is in an amount of 2-15 wt % claim 1 , the binder is in an amount of 5-25 wt % claim 1 , the silica source is in an amount of 10-30 wt % claim 1 , the zinc oxide is in an amount of 25-70 wt % claim 1 , the promoter metal is in an amount of 8-25 wt %.3. The adsorbing agent according to claim 1 , wherein the Si—Al ...

Acidic aromatization catalysts with improved activity and selectivity

Methods for producing supported catalysts containing a transition metal and a bound zeolite base are disclosed. These methods employ a step of impregnating the bound zeolite base with the transition metal, fluorine, and high loadings of chlorine. The resultant high chlorine content supported catalysts have improved catalyst activity in aromatization reactions.

METHOD OF PRODUCING ZEOLITE ENCAPSULATED NANOPARTICLES

The invention therefore relates to a method for producing zeolite, zeolite-like or zeotype encapsulated metal nanoparticles, the method comprises the steps of: 1) Adding one or more metal precursors to a silica or alumina source; 2) Reducing the one or more metal precursors to form metal nanoparticles on the surface of the silica or alumina source; 3) Passing a gaseous hydrocarbon, alkyl alcohol or alkyl ether over the silica or alumina supported metal nanoparticles to form a carbon template coated zeolite, zeolite-like or zeotype precursor composition; 4a) Adding a structure directing agent to the carbon template coated zeolite, zeolite-like or zeotype precursor composition thereby creating a zeolite, zeolite-like or zeotype gel composition; 4b) Crystallising the zeolite, zeolite-like or zeotype gel composition by subjecting said composition to a hydrothermal treatment; 5) Removing the carbon template and structure directing agent and isolating the resulting zeolite, zeolite-like or zeotype encapsulated metal nanoparticles. 1. A method for producing zeolite , zeolite-like or zeotype encapsulated metal nanoparticles , comprising:1) Adding one or more metal precursors to a silica or alumina source;2) Reducing the one or more metal precursors to form metal nanoparticles on the surface of the silica or alumina source;3) Passing a gaseous hydrocarbon, alkyl alcohol or alkyl ether over the silica or alumina supported metal nanoparticles to form a carbon template coated zeolite, zeolite-like or zeotype precursor composition;4a) Adding a structure directing agent to the carbon template coated zeolite, zeolite-like or zeotype precursor composition thereby creating a zeolite, zeolite-like or zeotype gel composition;4b) Crystallising the zeolite, zeolite-like or zeotype gel composition by subjecting said composition to a hydrothermal treatment; and5) Removing the carbon template and structure directing agent and isolating the resulting zeolite, zeolite-like or zeotype ...

CATALYST LOADING METHOD TO DISPERSE HEAT IN HYDROCONVERSION REACTOR

The invention relates to a method for modulating and controlling heat produced during an exothermic catalytic reaction. By combining two or more catalysts with differing activation energies, one can control the amount of heat change produced while the action proceeds. Among the advantages of such a process is the control of temperatures so that the change is within reactor tolerance. 1. A method for dispersing heat generated by a catalytic reaction comprising , combining at least two catalyst which have different activity temperatures and same functions in a catalysts being combines in a ratio sufficient to maintain an end of run temperature below a tolerance temperature of said reactor.2. The method of claim 1 , comprising admixing said at least two catalysts to form a uniform composition.3. The method of claim 1 , comprising providing a plurality of individual layers of said at least two catalysts in said catalytic reactor.4. The method of claim 1 , wherein said at least two catalysts are hydrocracking catalysts.5. The method of claim 1 , wherein at least one of said catalysts is an amorphous based catalyst claim 1 , and at least one of said catalysts is a zeolite based catalyst.6. The method of claim 5 , wherein said amorphous based catalyst contains Ni and Mo or Ni and W.7. The method of claim 1 , wherein at least one of said at least two catalysts contains Co and Mo claim 1 , Ni claim 1 , and Mo claim 1 , or Pt and Pd.8. The method of claim 1 , wherein said at least two catalysts are present in a range from 1/99 to 99/1 ratio.9. The method of claim 8 , wherein said at least two catalysts are an amorphous catalyst and a zeolite catalyst.{'claim-ref': {'@idref': 'CLM-00001', 'claim 1'}, 'The method of , wherein said catalytic reactor has a tolerance of from 25° C. to 40° C. higher than said activity temperature for one of said at least two catalysts having highest activity temperature of said at least two catalysts.'} The invention relates to methods for ...

DISORDERED MOLECULAR SIEVE SUPPORTS FOR THE SELECTIVE CATALYTIC REDUCTION OF NOx

A catalyst for selective catalytic reduction of NOhaving one or more transition metals selected from Cr, Mn, Fe, Co, Ce, Ni, Cu, Zn, Ga, Mo, Ru, Rh, Pd, Ag, In, Sn, Re, Ir, Pt, and mixtures thereof supported on a support, wherein the support has a molecular sieve having at least one intergrowth phase having at least two different small-pore, three-dimensional framework structures. 1. A catalyst for selective catalytic reduction of NOcomprising:a. one or more transition metals selected from the group consisting of Cr, Mn, Fe, Co, Ce, Ni, Cu, Zn, Ga, Mo, Ru, Rh, Pd, Ag, In, Sn, Re, Ir, Pt, and mixtures thereof, andb. a support comprising an aluminosilicate, a silico-aluminophosphate, or aluminosilicate/silico-aluminophosphate molecular sieve having an intergrowth phase comprising an AEI framework,wherein the one or more transition metals are disposed inside the pores of the molecular sieve, on the external surface of the molecular sieve, or both inside the pores and on the external surface of the molecular sieve, andwherein said transition metal is present in an amount of about 0.01 to about 6 weight percent, based on the total weight of the molecular sieve.2. The catalyst of claim 1 , wherein the AEI framework structure is present in a ratio of about 1:99 to 99:1 with respect to other frameworks in the molecular sieve.3. The catalyst of claim 1 , wherein the AEI framework structure is present in a ratio of about 5:95 to about 15:85 with respect to other frameworks in the molecular sieve.4. The catalyst of claim 1 , wherein the molecular sieve is an aluminosilicate.5. The catalyst of claim 1 , wherein the molecular sieve is a silico-aluminophosphates.6. The catalyst of claim 1 , wherein said transition metal is selected from the group consisting of Cu claim 1 , Fe claim 1 , Co claim 1 , Pt claim 1 , and Mn.7. The catalyst of claim 1 , wherein said transition metal is Cu.8. The catalyst of claim 1 , wherein said transition metal is present in an amount of about 1 to ...

SPINEL COMPOSITIONS AND APPLICATIONS THEREOF

Spinels having a general formula of ABO, where A and B are a transition metal but not the same transition metal are disclosed. Spinel and spinel compositions of the application are useful in various applications and methods as further described. 1. A catalyst comprising a spinel having the general formula of ABO , wherein A and B are a transition metal , wherein A and B are not the same transition metal.2. The catalyst of claim 1 , wherein the transition metal is selected from the group consisting of iron (Fe) claim 1 , manganese (Mn) claim 1 , nickel (Ni) claim 1 , cobalt (Co) claim 1 , copper (Cu) claim 1 , vanadium (V) claim 1 , silver (Ag) claim 1 , palladium (Pd) claim 1 , ruthenium (Ru) claim 1 , rhodium (Rh) claim 1 , platinum (Pt) claim 1 , molybdenum (Mo) claim 1 , niobium (Nb) claim 1 , titanium (Ti) claim 1 , etc.) and an “other metal” (i.e. claim 1 , aluminum (Al) claim 1 , magnesium (Mg) claim 1 , gallium (Ga) claim 1 , tin (Sn) claim 1 , thallium (Tl) claim 1 , lead (Pb) claim 1 , bismuth (Bi) claim 1 , and indium (In).3. The catalyst of claim 1 , wherein the spinel is rare-earth metal free.4. The catalyst of claim 1 , wherein the spinel further comprises a dopant.5. The catalyst of claim 4 , wherein the spinel has a general formula of ADBO claim 4 , where D is the dopant.7. The catalyst of claim 4 , wherein the dopant is a low valence dopant.8. The catalyst of claim 4 , wherein the dopant is a high valence dopant.9. The catalyst of claim 1 , wherein the spinel is deposited on a substrate.10. The catalyst of claim 9 , wherein the substrate is a support oxide.11. The catalyst of claim 10 , wherein the support oxide is transition alumina claim 10 , alpha alumina claim 10 , titania claim 10 , zeolite claim 10 , silica claim 10 , silicate claim 10 , magnesium-silicate claim 10 , silica-alumina claim 10 , ceria claim 10 , ceria-zirconia claim 10 , lanthanide-doped ceria-zirconia claim 10 , lanthanum doped alumina claim 10 , and mixed metal oxide.12. The ...

Acidic Aromatization Catalyst with Improved Activity and Stability

Methods for producing supported catalysts containing a transition metal and a bound zeolite base are disclosed. These methods employ a step of impregnating the bound zeolite base with the transition metal, fluorine, and high loadings of chlorine. The resultant high chlorine content supported catalysts have improved catalyst activity in aromatization reactions. 116-. (canceled)17. A method of producing a supported catalyst , the method comprising:(a) impregnating a bound zeolite base with a transition metal precursor, a chlorine precursor, and a fluorine precursor to form an impregnated zeolite base; and(b) drying and then calcining the impregnated zeolite base to produce the supported catalyst; wherein the supported catalyst comprises, based on the total weight of the supported catalyst:from about 0.3 wt. % to about 3 wt. % of a transition metal;from about 1.8 wt. % to about 4 wt. % of chlorine; andfrom about 0.4 wt. % to about 1.5 wt. % of fluorine; andwherein the supported catalyst is characterized by a peak reduction temperature on a Temperature Programmed Reduction curve in a range from about 580° F. to about 800° F.18. The method of claim 17 , wherein impregnating the bound zeolite base with the transition metal precursor claim 17 , the chlorine precursor claim 17 , and the fluorine precursor comprises mixing the bound zeolite base with an aqueous solution comprising the transition metal precursor claim 17 , the chlorine precursor claim 17 , and the fluorine precursor.19. The method of claim 17 , wherein the method further comprises a reducing step after the drying and calcining of the impregnated zeolite base claim 17 , the reducing step comprising contacting the supported catalyst with a reducing gas stream to produce an activated catalyst.20. The method of claim 19 , wherein the activated catalyst comprises from about 0.2 wt. % to about 1.3 wt. % of chlorine claim 19 , based on the total weight of the activated catalyst.21. An activated aromatization ...

CATALYTIC HYDROCARBON DEHYDROGENATION

A catalyst for dehydrogenation of hydrocarbons includes a support including zirconium oxide and Linde type L zeolite (L-zeolite). A concentration of the zirconium oxide in the catalyst is in a range of from 0.1 weight percent (wt. %) to 20 wt. %. The catalyst includes from 5 wt. % to 15 wt. % of an alkali metal or alkaline earth metal. The catalyst includes from 0.1 wt. % to 10 wt. % of tin. The catalyst includes from 0.1 wt. % to 8 wt. % of a platinum group metal. The alkali metal or alkaline earth metal, tin, and platinum group metal are disposed on the support. 1. A catalyst for dehydrogenation of hydrocarbons , the catalyst comprising:a support comprising zirconium oxide and Linde type L zeolite (L-zeolite), wherein a concentration of the zirconium oxide in the catalyst is in a range of from 0.1 weight percent (wt. %) to 20 wt. %;from 5 wt. % to 15 wt. % of an alkali metal or alkaline earth metal, the alkali metal or alkaline earth metal disposed on the support;from 0.1 wt. % to 10 wt. % of tin, the tin disposed on the support; andfrom 0.1 wt. % to 8 wt. % of a platinum group metal, the platinum group metal disposed on the support.2. The catalyst of claim 1 , wherein the alkali metal or alkaline earth metal is selected from the group consisting of lithium claim 1 , sodium claim 1 , potassium claim 1 , rubidium claim 1 , cesium claim 1 , beryllium claim 1 , magnesium claim 1 , calcium claim 1 , and barium.3. The catalyst of claim 2 , wherein the alkali metal is potassium or cesium.4. The catalyst of claim 2 , wherein the platinum group metal is selected from the group consisting of platinum claim 2 , ruthenium claim 2 , iridium claim 2 , rhodium claim 2 , and palladium.5. The catalyst of claim 2 , wherein the catalyst is configured to dehydrogenate hydrocarbons including 3 to 6 carbon atoms at an operating temperature in a range of from about 500 degrees Celsius (° C.) to about 800° C. and an operating pressure in a range of from about 0.01 bar to about 10 bar.6. ...

NOBLE METAL-MOLECULAR SIEVE CATALYSTS

Exhaust gas catalysts are disclosed. One exhaust gas catalyst comprises a noble metal and a molecular sieve, and has an infrared spectrum having a characteristic absorption peak from 750 cmto 1050 cmin addition to the absorption peaks for the molecular sieve itself. The exhaust gas catalyst also comprises a noble metal and a molecular sieve, having greater than 5 percent of the noble metal amount located inside pores of the molecular sieve. The exhaust gas catalyst also comprises a first and second molecular sieve catalyst. The first molecular sieve catalyst comprises a first noble metal and a first molecular sieve, and the second molecular sieve catalyst comprises a second noble metal and a second molecular sieve. The first and second molecular sieves are different. The invention also includes exhaust systems comprising the exhaust gas catalysts, and a method for treating exhaust gas utilizing the exhaust gas catalysts. 1. An exhaust gas catalyst effective to adsorb NOand hydrocarbons (HC) at or below a low temperature and to convert and release the adsorbed NOand HC at temperatures above the low temperature , said exhaust gas catalyst comprising a first molecular sieve catalyst and a second molecular sieve catalyst , wherein the first molecular sieve catalyst comprises a first noble metal and a first molecular sieve , and the second molecular sieve catalyst comprises a second noble metal and a second molecular sieve , wherein the first molecular sieve is different than the second molecular sieve.2. The exhaust gas catalyst of wherein greater than 5 percent of the total amount of first noble metal is located inside pores of the first molecular sieve and greater than 5 percent of the total amount of second noble metal is located inside pores of the second molecular sieve.3. The exhaust gas catalyst of wherein the first noble metal and the second noble metal are independently selected from the group consisting of platinum claim 1 , palladium claim 1 , rhodium claim 1 ...

Manganese-Containing Diesel Oxidation Catalyst

An oxidation catalyst composite, methods, and systems for the treatment of exhaust gas emissions from a diesel engine are described. More particularly, an oxidation catalyst composite including a first washcoat layer comprising a Pt component and a Pd component, and a second washcoat layer including a refractory metal oxide support containing manganese, a zeolite, and a platinum component is described.

COATED SUBSTRATES FOR USE IN CATALYSIS AND CATALYTIC CONVERTERS AND METHODS OF COATING SUBSTRATES WITH WASHCOAT COMPOSITIONS

Disclosed are, inter alia, methods of forming coated substrates for use in catalytic converters, as well as washcoat compositions and methods suitable for using in preparation of the coated substrates, and the coated substrates formed thereby. The catalytic material is prepared by a plasma-based method, yielding catalytic material with a lower tendency to migrate on support at high temperatures, and thus less prone to catalyst aging after prolonged use. Also disclosed are catalytic converters using the coated substrates, which have favorable properties as compared to catalytic converters using catalysts deposited on substrates using solution chemistry. Also disclosed are exhaust treatment systems, and vehicles, such as diesel vehicles, particularly light-duty diesel vehicles, using catalytic converters and exhaust treatment systems using the coated substrates. 1. A coated substrate comprising:a substrate;a washcoat layer comprising zeolite particles; anda washcoat layer comprising catalytically active particles;wherein the catalytically active particles comprise plasma synthesized composite nano-particles bonded to micron-sized carrier particles, and the composite nano-particles comprise a support nano-particle and a catalytic nano-particle.242-. (canceled)43. A washcoat composition comprising a solids content of:35% to 95% by weight of catalytically active particles comprising plasma synthesized composite nano-particles bonded to micron-sized carrier particles, and the composite nano-particles comprise a support nano-particle and a catalytic nano-particle;2% to 5% by weight of boehmite particles; and2% to 55% by weight of metal-oxide particles.4492-. (canceled)93. A method of forming a washcoat composition comprising:plasma synthesizing composite nano-particles comprising a support nano-particle and a catalytic nano-particle;bonding the plasma synthesized composite nano-particles to micron-sized carrier particles to form catalytically active particles; ...

CATALYST DESIGN FOR HEAVY-DUTY DIESEL COMBUSTION ENGINES

Disclosed are washcoats, coated substrates formed from such washcoats, and catalytic converters for use in diesel applications, such as heavy duty diesel applications. Methods of preparing the coated substrates are also disclosed. 196-. (canceled)97. A method of forming a coated substrate , comprising:coating a substrate with a first washcoat layer comprising zeolites;coating the first washcoat layer with a second washcoat layer comprising a first catalytically active material comprising first composite nanoparticles embedded within porous micron-sized carrier particles, wherein the first composite nanoparticles comprise a first support nanoparticle and a first catalytic nanoparticle, and wherein the first catalytic nanoparticle comprises a platinum-palladium alloy; andcoating the second washcoat layer with a third washcoat layer comprising a second catalytically active material comprising second composite nanoparticles embedded within porous micron-sized carrier particles, wherein the second composite nanoparticles comprise a second support nanoparticle and a second catalytic nanoparticle, and wherein the second catalytic nanoparticle comprises a platinum-palladium alloy.98. The method of claim 97 , wherein the platinum-palladium alloy of the first catalytic nanoparticle comprises a platinum:palladium ratio of less than about 4:1 Pt:Pd.99. The method of claim 98 , wherein the platinum-palladium alloy of the first catalytic nanoparticle comprises a platinum:palladium ratio of about 1:1 to about 4:1 Pt:Pd.100. The method of claim 97 , wherein the platinum-palladium alloy of the second catalytic nanoparticle comprises a platinum:palladium ratio of greater than about 4:1 Pt:Pd.101. The method of claim 100 , wherein the platinum palladium alloy of the second catalytic nanoparticle comprises a platinum:palladium ratio of about 10:1 to about 100:1 Pt:Pd.102. The method of claim 100 , wherein the platinum-palladium alloy of the first catalytic nanoparticle comprises a ...

Addition of a Base to Enhance Product Yield in Alkylation Reactions

A process for making styrene including providing toluene, a co-feed, and a C 1 source to a reactor containing a catalyst having acid sites and reacting toluene with the C 1 source in the presence of the catalyst and the co-feed to form a product stream containing ethylbenzene and styrene, wherein the C 1 source is selected from methanol, formaldehyde, formalin, trioxane, methylformcel, paraformaldehyde, methylal, dimethyl ether, and wherein the co-feed removes at least a portion of the acid sites on the catalyst. The co-feed can be selected from the group of aniline, amines, cresol, anisol, and combinations thereof.

COMPOSITION OF MATTER AND STRUCTURE OF ZEOLITE UZM-55 AND USE IN ISOMERIZATION OF AROMATIC MOLECULES

Isomerization processes such as the isomerization of ethylbenzene and xylenes, are catalyzed by the new crystalline aluminosilicate zeolite comprising a novel framework type that has been designated UZM-55. This zeolite is represented by the empirical formula: 4. The process of wherein x is less than 0.02.5. The process of wherein y is less than 0.02.6. The process of wherein r is from about 0.0005 to about 0.08.7. The process of wherein the microporous crystalline zeolite is thermally stable up to a temperature of at least 600° C.8. The process of wherein the microporous crystalline zeolite has an SiO/AlOratio greater than 75.9. The process of wherein the microporous crystalline zeolite has an SiO/AlOratio greater than 150.10. The process of wherein the microporous crystalline zeolite M is selected from the group consisting of lithium claim 1 , potassium claim 1 , rubidium claim 1 , cesium claim 1 , magnesium claim 1 , calcium claim 1 , strontium claim 1 , barium claim 1 , zinc claim 1 , yttrium claim 1 , lanthanum and gadolinium.11. The process of wherein the microporous crystalline zeolite R is 1 claim 1 ,6-bis(N-methylpiperidinium)hexane.12. The process of wherein the microporous crystalline zeolite has a micropore volume of greater than 0.08 mL/g and less than 0.15 mL/g.13. The process of wherein the isomerization conditions include a temperature of about 300° C. to about 450° C.14. The process of wherein the isomerization conditions include a pressure of about 70 psig to about 130 psig.15. The process of wherein the isomerization conditions include a weight hourly space velocity of about 5 hto about 7 h.16. The process of wherein the feed stream also comprises hydrogen and one or more xylenes selected from the group consisting of p-xylene claim 1 , m-xylene claim 1 , o-xylene and combinations thereof.17. The process of wherein the catalyst also comprises a hydrogenation function selected from a noble metal and a base metal claim 1 , and a binder.18. The ...

Catalyst Compositions, Articles, Methods And Systems

Described are catalyst compositions, catalytic articles, exhaust gas treatment systems and methods that utilize the catalytic articles. The catalyst composition comprises a washcoat including a zeolite, refractory metal oxide support particles, and a platinum group metal supported on the refractory metal oxide support particles. Greater than 90% of the refractory metal oxide particles supporting PGM have a particle size greater than 1 μm and a d 50 less than 40 microns.

Catalyst for Preparing Isobutene by Dissociation of Methyl Tert-Butyl Ether, Preparation Method and Use Thereof

Disclosed is a catalyst for preparing isobutene by dissociation of methyl tert-butyl ether, the catalyst comprising amorphous silica alumina and a silicalite-1 molecular sieve, wherein the total IR acid amount of weak acids in the catalyst is in a range from 0.020 to 0.080 mmol/g, and the ratio of B acid/L acid of the weak acids is in a range from 2.5:1 to 4.0:1. Also provided is a method of preparing the catalyst and the use thereof. The catalyst has a high selectivity with respect to isobutene, and high conversion of methyl tert-butyl ether, and can also effectively inhibit formation of the by-product dimethyl ether. 1. A catalyst for preparing isobutene by dissociation of methyl tert-butyl ether , the catalyst comprising amorphous silica alumina and a silicalite-1 molecular sieve , wherein the total IR acid amount of weak acids in the catalyst is in a range from 0.020 to 0.080 mmol/g , and the ratio of B acid/L acid of the weak acids is in a range from 2.5:1 to 4.0:1.2. The catalyst of claim 1 , wherein the mass ratio of the amorphous silica-alumina to the silicalite-1 is in a range from 9.5:1 to 1:1.3. The catalyst of claim 2 , wherein the mass ratio of the amorphous silica-alumina to the silicalite-1 is in a range from 8:1 to 4:1.4. The catalyst of claim 1 , wherein in said amorphous silica-alumina claim 1 , the content of SiOis in a range from 60 wt % to 99 wt % claim 1 , and the content of AlOis in a range from 1 wt % to 40 wt %.5. The catalyst of claim 4 , wherein in said amorphous silica-alumina claim 4 , the content of silica is in a range from 80 wt % to 95 wt % claim 4 , and the content of alumina is in a range from 5 wt % to 20 wt %.6. The catalyst of claim 1 , wherein the catalyst further comprises an active metal component claim 1 , which is at least one selected from the group consisting of Group IIA metals and Group VIII metals.7. The catalyst of claim 6 , wherein the content of said active metal component on the basis of the active metal in the ...

Method for producing hydrocarbon liquid fuel

A method for producing a hydrocarbon liquid fuel including hydrocracking a raw material oil in the presence of a hydrocracking catalyst, at a supplying pressure of hydrogen of from 0.1 to 1.0 MPa, a liquid space velocity of liquid volume of the raw material oil of from 0.05 to 10.0 hr −1 , and a flow rate of the hydrogen from 50 to 3,000 NL per 1 L of the raw material oil, wherein the hydrocracking catalyst is produced by a method including stirring a sulfur compound and a cracking catalyst in an aqueous medium to allow liquid-solid separation (step 1); stirring a solid product obtained in the step 1 and a metal component in an aqueous medium to allow liquid-solid separation (step 2); baking a solid product obtained in the step 2 (step 3); and reducing a solid product obtained in the step 3, or reducing a solid product obtained in the step 3, and then subjecting a reduced product to sulfurization treatment (step 4). According to the present invention, the hydrocracking of a raw material oil such as fats and oils and biomass retort oils, or a hydrocarbon or the like in petroleum oils, in a given composition can be accomplished by supplying a low-pressure hydrogen of a normal pressure or so.

COPPER-BASED CATALYST FOR CONVERTING AMMONIA INTO NITROGEN

A copper-based catalyst which is suitable for converting ammonia of high concentration and with better selectivity, thereby solving a problem of pollution and toxicity due to nitrogen oxides by a conventional catalyst reacting under high temperature is disclosed. The copper-based catalyst comprises: a porous oxide support and a low valent copper compound mixing with the porous oxide support by an acid hydrothermal method; wherein the low valent copper compound with is Cu and CuO. 1. A copper-based catalyst for converting ammonia into nitrogen comprising:a porous oxide support; anda copper compound with low valence mixing with the porous oxide support by an acid hydrothermal method;{'sub': '2', 'wherein the low valent copper compound is Cu and CuO.'}2. The copper-based catalyst for converting ammonia nitrogen as defined in claim 1 , wherein the porous oxide support adheres to low valent copper compounds with a weight percentage of 20˜40%.3. The copper-based catalyst for converting ammonia into nitrogen as defined in claim 1 , wherein the porous oxide support is aluminum oxide claim 1 , silicon oxide claim 1 , clays or zeolitest. 1. Field of the InventionThe present invention generally relates to a copper-based catalyst for converting ammonia (NH) into nitrogen and, more particularly, to a copper-based catalyst with better selectivity and suitable for converting ammonia (NH) of high concentration.2. Description of the Related ArtWaste resin generated by industries can be wet treated to produce ammonia with concentration up to 66.7%. Ammonia can be decomposed by a catalytic decomposition method. There are two kinds of catalytic decomposition methods for ammonia, which are reduction reaction and oxidation reaction. The reduction decomposition method mainly produces hydrogen and nitrogen, but is energy-waste due to its high reaction temperature. The oxidation decomposition method mainly produces nitrogen and water. Nitrogen produced by the oxidation decomposition method ...

OXIDATION CATALYST FOR A DIESEL ENGINE EXHAUST

An oxidation catalyst is described for treating an exhaust gas produced by a diesel engine comprising a catalytic region and a substrate, wherein the catalytic region comprises a catalytic material comprising: bismuth (Bi) or an oxide thereof; an alkali metal or an oxide thereof; a platinum group metal (PGM) selected from the group consisting of (i) platinum (Pt), (ii) palladium (Pd) and (iii) platinum (Pt) and palladium (Pd); and a support material comprising a mixed oxide of alumina and silica, a mixed oxide of silica and a refractory oxide, a composite oxide of alumina and silica, a composite oxide of silica and a refractory oxide, alumina doped with a silica or silica doped with a refractory oxide. 1. An oxidation catalyst for treating an exhaust gas produced by a diesel engine comprising a catalytic region and a substrate , wherein the catalytic region comprises a catalytic material comprising:bismuth (Bi) or an oxide thereof;an alkali metal or an oxide thereof;a platinum group metal (PGM) selected from the group consisting of (i) platinum (Pt), (ii) palladium (Pd) and (iii) platinum (Pt) and palladium (Pd); anda support material comprising a mixed oxide of alumina and silica, a mixed oxide of silica and a refractory oxide, a composite oxide of alumina and silica, a composite oxide of silica and a refractory oxide, alumina doped with a silica or silica doped with a refractory oxide.2. An oxidation catalyst according to claim 1 , wherein the support material comprises alumina doped with silica in a total amount of 0.5 to 15% by weight of the alumina.3. An oxidation catalyst according to claim 1 , wherein the bismuth or an oxide thereof is supported on the support material.4. An oxidation catalyst according to claim 1 , wherein the alkali metal or an oxide thereof is disposed or supported on the support material.5. An oxidation catalyst according to claim 1 , wherein the alkali metal is caesium (Cs).6. An oxidation catalyst according to claim 1 , wherein the ...

Reusable porous Na(Si2Al)O6.xH2O/NiFe2O4 structure for selective removal of heavy metals from waste waters

The 3-Glycidoxypropyltrimethoxysilane (GPTMS) decorated magnetic more-aluminosilicate shell Na(SiAl)O.xHO/NiFeOstructures were hydrothermally prepared and were well characterized by different analysis methods. The XRD patterns were truly proved the formation of the aluminosilicate layer on the surface of the magnetic cores. In addition to the TGA curve which implied on the presence of the GPTMS organic segment, nitrogen adsorption-desorption isotherms demonstrated that the final sample has high specific surface area. The products were incredibly able to remove the toxic lead and cadmium ions from the wastewaters. Furthermore, the mechanism of the sorption and the role of GPTMS in enhancing the sorption capacity of the structures were comprehensively discussed. 1- A method of making a high capacity reusable magnetic core-aluminosilicate shell sorbent for selective purification of wastewaters containing heavy metal ions , comprising the steps of:{'sub': 3', '2', '3, 'sup': 2+', '3+, 'a) preparing 50 ml transparent solution containing Ni(NO)and FeCl(corresponding to Ni/Fe molar ratio of 1:2);'}b) adding said transparent solution to NaOH solution 2 M drop by drop under vigorous stirring;c) adding a mixture containing sufficient amount of EG and TMAOH the solution of step b, above suspension drop wise;d) Stirring the above combined mixture in step c for 2 hrs, then immediately transferring it into an autoclave and keeping it at 200° C. for 8 hrs;e) Collecting black solid particles by an external magnet, repeatedly washing said particles with de-ionized water, and drying them at 80° C. for 6 hrs.2- The method of claim 1 , further comprising the steps of preparing Na(SiAl)O.xHO/NiFeOparticles as follows:{'sub': 3', '3', '2, 'f) dissolving Al(NO).9HO in 30 mL of NaOH 2 M containing 0.9 g of cetyl trimethylammonium bromide (CTAB) and 5.05 mL of tetraethyl orthosilicate (TEOS);'}g) then magnetically stirring it for 90 min;h) Dispersing Magnetic particles (1.0 g) of the above ...

Catalyst Design for Heavy-Duty Diesel Combustion Engines

Disclosed are washcoats, coated substrates formed from such washcoats, and catalytic converters for use in diesel applications, such as heavy duty diesel applications. Methods of preparing the coated substrates are also disclosed. 1. The coated substrate of claim 5 , wherein the coated substrate is free of zeolites claim 5 , first catalytically active material further comprises plasma-created composite nanoparticles bonded to or embedded within micron-sized carrier particles claim 5 , the composite nanoparticles comprising a support nanoparticle and a catalytic nanoparticle claim 5 , and the second catalytically active material further comprises plasma-created composite nanoparticles bonded to or embedded within micron-sized carrier particles claim 5 , the composite nanoparticles comprising a support nanoparticle and a catalytic nanoparticle.2. (canceled)3. The coated substrate of claim 5 , wherein the coated substrate is free of zeolites claim 5 , and wherein the first catalytically active material comprises plasma-created composite nanoparticles bonded to or embedded within micron-sized carrier particles claim 5 , the composite nanoparticles comprising a support nanoparticle and a catalytic nanoparticle.4. (canceled)5. A coated substrate comprising:a substrate; boehmite particles; and', 'a first catalytically active material comprising platinum and palladium in a weight ratio of 10:1 platinum:palladium to 100:1 platinum:palladium, or comprising platinum and no palladium; and, 'a first washcoat layer comprising boehmite particles; and', 'a second catalytically active material comprising platinum and palladium in a weight ratio of 1:2 platinum:palladium to 8:1 platinum:palladium, or comprising two or more catalytically active materials which together comprise platinum and palladium in a weight ratio of 1:2 platinum:palladium to 8:1 platinum:palladium, or comprising palladium and no platinum., 'a second washcoat layer comprising6. (canceled)7. The coated substrate of ...

Alkylation Process Using a Catalyst Comprising Cerium Rich Rare Earth Containing Zeolites and a Hydrogenation Metal

An improved alkylation process utilizing a solid-acid catalyst comprising a cerium rich rare earth containing zeolite and a hydrogenation metal is disclosed. 1. A process for alkylating hydrocarbons wherein an alkylatable organic compound is reacted with an alkylation agent to form an alkylate in the presence of a catalyst with the catalyst being subjected intermittently to a regeneration step by being contacted with a feed containing a saturated hydrocarbon and hydrogen , said regeneration being carried out at 90% or less of the active cycle of the catalyst , with the active cycle of the catalyst being defined as the time from the start of the feeding of the alkylation agent to the moment when , in comparison with the entrance of the catalyst-containing reactor section , 20% of the alkylation agent leaves the catalyst-containing reactor section without being converted , not counting isomerization inside the molecule , wherein said catalyst comprises a hydrogenating function , solid acid constituent and one or more rare earth elements , said one or more rare earth elements comprising at least 0.1 wt % cerium calculated as fraction of the total catalyst weight.2. A process according to claim 1 , wherein the one or more rare earth elements comprise at least 0.3 wt % cerium claim 1 , calculated as fraction of the total catalyst weight.3. A process according to claim 1 , wherein the one or more rare earth elements comprise at least 0.5 wt % cerium calculated as fraction of the total catalyst weight.4. A process according to claim 1 , wherein the one or more rare earth elements are comprised of cerium and lanthanum.5. A process according to claim 1 , wherein the cerium is added to the catalyst and/or the solid acid constituent either by impregnation or by ion exchange or a combination of the two.6. The process of wherein the alkylatable organic compound comprises an isoparaffin or mixture of isoparaffins and the alkylation agent comprises C3-C5 alkenes or mixture of C3- ...

COATED SUBSTRATES FOR USE IN CATALYSIS AND CATALYTIC CONVERTERS AND METHODS OF COATING SUBSTRATES WITH WASHCOAT COMPOSITIONS

Disclosed are, inter alia, methods of forming coated substrates for use in catalytic converters, as well as washcoat compositions and methods suitable for using in preparation of the coated substrates, and the coated substrates formed thereby. The catalytic material is prepared by a plasma-based method, yielding catalytic material with a lower tendency to migrate on support at high temperatures, and thus less prone to catalyst aging after prolonged use. Also disclosed are catalytic converters using the coated substrates, which have favorable properties as compared to catalytic converters using catalysts deposited on substrates using solution chemistry. Also disclosed are exhaust treatment systems, and vehicles, such as diesel vehicles, particularly light-duty diesel vehicles, using catalytic converters and exhaust treatment systems using the coated substrates. 1. A coated substrate comprising:a substrate;a washcoat layer comprising zeolite particles; anda washcoat layer comprising catalytically active particles;wherein the catalytically active particles comprise plasma synthesized composite nano-particles bonded to micron-sized carrier particles, and the composite nano-particles comprise a support nano-particle and a catalytic nano-particle, the catalytic nano-particle comprising at least one platinum group metal.2. The coated substrate of claim 1 , wherein the washcoat layer comprising zeolite particles is formed on top of the washcoat layer comprising catalytically active particles.3. The coated substrate of claim 1 , wherein the washcoat layer comprising catalytically active particles is formed on top of the washcoat layer comprising zeolite particles.4. (canceled)5. The coated substrate of claim 1 , wherein the catalytic nano-particles comprise platinum and palladium.6. The coated substrate of claim 5 , wherein the catalytic nano-particles comprise platinum and palladium in a weight ratio of 2:1 platinum:palladium.7. The coated substrate of claim 1 , wherein the ...

Pgm catalyst for treating exhaust gas

Provided are catalysts comprising a small pore molecular sieve embedded with PGM and methods for treating lean burn exhaust gas using the same.

OXIDATION CATALYST FOR A DIESEL ENGINE EXHAUST

An oxidation catalyst for treating an exhaust gas produced by a diesel engine comprises a catalytic region and a substrate, wherein the catalytic region comprises a catalytic material comprising: bismuth (Bi) or an oxide thereof; a Group 8 metal or an oxide thereof; a platinum group metal (PGM) selected from the group consisting of (i) platinum (Pt), (ii) palladium (Pd) and (iii) platinum (Pt) and palladium (Pd); and a support material, which comprises alumina, silica, a mixed oxide of alumina and a refractory oxide, a mixed oxide of silica and a refractory oxide, a composite oxide of alumina and a refractory oxide, a composite oxide of silica and a refractory oxide, alumina doped with a refractory oxide or silica doped with a refractory oxide. 1. An oxidation catalyst for treating an exhaust gas produced by a diesel engine comprising a catalytic region and a substrate , wherein the catalytic region comprises a catalytic material comprising:bismuth (Bi) or an oxide thereof;a Group 8 metal or an oxide thereof;a platinum group metal (PGM) selected from the group consisting of (i) platinum (Pt), (ii) palladium (Pd) and (iii) platinum (Pt) and palladium (Pd); anda support material, which comprises alumina, silica, a mixed oxide of alumina and a refractory oxide, a mixed oxide of silica and a refractory oxide, a composite oxide of alumina and a refractory oxide, a composite oxide of silica and a refractory oxide, alumina doped with a refractory oxide or silica doped with a refractory oxide.2. An oxidation catalyst according to claim 1 , wherein the support material comprises alumina doped with silica in a total amount of 0.5 to 15% by weight of the alumina.3. An oxidation catalyst according to claim 1 , wherein the refractory oxide is selected from the group consisting of silica claim 1 , titania and ceria.4. An oxidation catalyst according to claim 1 , wherein the refractory oxide is zirconia.5. An oxidation catalyst according to claim 1 , wherein the bismuth or an ...

OXIDATION CATALYST FOR A DIESEL ENGINE EXHAUST

An oxidation catalyst is described for treating an exhaust gas produced by a diesel engine comprising a catalytic region and a substrate, wherein the catalytic region comprises a catalytic material comprising: bismuth (Bi) or an oxide thereof; a platinum group metal (PGM) selected from the group consisting of (i) platinum (Pt), (ii) palladium (Pd) and (iii) platinum (Pt) and palladium (Pd); and a support material comprising a mixed oxide of titanium dioxide and silica; or a composite oxide of titanium dioxide and silica; or titanium dioxide doped with silica; wherein the platinum group metal (PGM) is supported on the support material; and wherein the bismuth (Bi) or an oxide thereof is supported on the support material. 1. An oxidation catalyst for treating an exhaust gas produced by a diesel engine comprising a catalytic region and a substrate , wherein the catalytic region comprises a catalytic material comprising:bismuth (Bi) or an oxide thereof;a platinum group metal (PGM) selected from the group consisting of (i) platinum (Pt), (ii) palladium (Pd) and (iii) platinum (Pt) and palladium (Pd); anda support material comprising a mixed oxide of titanium dioxide and silica; or a composite oxide of titanium dioxide and silica; or titanium dioxide doped with silica;wherein the platinum group metal (PGM) is supported on the support material; andwherein the bismuth (Bi) or an oxide thereof is supported on the support material.2. An oxidation catalyst according to claim 1 , wherein the support material comprises either (i) the mixed oxide of titanium dioxide and silica or (ii) the composite oxide of titanium dioxide and silica; wherein the support material comprises 1 to 50% by weight of silica.3. An oxidation catalyst according to claim 1 , wherein the support material comprises titanium dioxide doped with silica in a total amount of 0.1 to 35% by weight.4. An oxidation catalyst according to claim 1 , wherein the catalytic region has a total loading of bismuth of 1 to ...

DIESEL EXHAUST GAS PURIFICATION CATALYST AND DIESEL EXHAUST GAS PURIFICATION SYSTEM

A diesel exhaust gas purification catalyst contains a substrate, and a catalyst layer formed on the substrate. The catalyst layer contains a carrier, a noble metal and/or an oxide thereof supported by the carrier, and a composite oxide of cerium and one or more Group III and/or Group IV elements. The diesel exhaust gas purification catalyst when in use is disposed on an upstream side of an exhaust gas stream with respect to a denitration catalyst. 111.-. (canceled)12. A diesel exhaust gas purification catalyst , comprising:a substrate;a catalyst layer formed on the substrate, the catalyst layer comprising a carrier, a noble metal and/or an oxide thereof supported by the carrier, and a composite oxide of cerium and one or more Group III and/or Group IV elements; anda first part to which exhaust gas is fed and a second part to which the exhaust gas that has passed through the first part is fed, the first part comprising a smaller content of the composite oxide per unit volume than that of the second part, wherein the catalyst when in use is disposed on an upstream side of an exhaust gas stream with respect to a denitration catalyst.131. The diesel exhaust gas purification catalyst according to claim , the catalyst layer comprising:a first catalyst layer formed on the substrate; anda second catalyst layer formed on the first layer, the second catalyst layer comprising a larger content of the composite oxide per unit volume than that of the first catalyst layer.141. The diesel exhaust gas purification catalyst according to claim , wherein the composite oxide comprises the Group III element , and the Group III element is a lanthanoid and/or an actinoid.151. the diesel exhaust gas purification catalyst according to claim , wherein the composite oxide comprises the Group III element , and the Group III element is lanthanum and/or praseodymium.161. The diesel exhaust gas purification catalyst according to claim , wherein the ratio of the cerium in the composite oxide is in ...

METHOD FOR METHANOL CONVERSION TO PROPYLENE OVER A MONOLITHIC CATALYST SYSTEM

A catalyst system and a process for methanol to light olefin conversion with enhanced selectivity towards propylene. The catalyst system comprises a honeycomb monolith catalyst support coated with aluminosilicate nanozeolite catalysts on the edges and inside the channels of the support structure. The aluminosilicate nanozeolite catalysts have not been pre-modified with a promoter metal. The catalyst system gives higher hydrothermal stability to the catalyst compared to randomly packed pellet catalysts and allows methanol to be converted to predominantly propylene at a low temperature, with decreased selectivity towards C, higher olefins and paraffinic hydrocarbons. 1. A method for converting methanol into light olefins , comprising:passing the methanol in the vapor phase through a catalyst system for a time and at a temperature effective for converting the methanol to propylene with a selectivity towards propylene of at least 40% relative to a total mass of light olefin products and a selectivity towards propylene that is greater than a selectivity towards ethylene relative to a total mass of light olefin products and that is greater than a selectivity towards butylene relative to a total mass of light olefin products, 7-12 wt % of the zeolite nanoparticles relative to the total weight of the catalyst system of zeolite nanoparticles having a silica to alumina molar ratio of 260-5000 in the form of crystals having an average particle diameter of 10-50 nm; and', 'a honeycomb monolith support with 500-1200 cells per square inch coated with the zeolite nanoparticles on the edges and inside the channels of the honeycomb monolith support;', 'wherein the zeolite nanoparticles are not modified with a promoter metal., 'wherein the catalyst system comprises2. The method of claim 1 , wherein the zeolite nanoparticles are microporous molecular sieves having an MFI framework type claim 1 , which have a BET surface area of 100-1000 mgand which have a pore size distribution of 0.6 ...

Low temperature catalyst/hydrocarbon trap

A low-temperature catalyst is provided for reducing cold-start hydrocarbon emissions. The catalyst comprises a platinum group metal impregnated onto an oxygen storage material. The catalyst may be used alone or may be included in a hydrocarbon trap containing a hydrocarbon adsorption material therein. The catalyst/hydrocarbon trap is positioned in the exhaust system of a vehicle downstream from a close-coupled catalyst such that the exhaust temperature at the catalyst location does not exceed 850° C. during normal vehicle operation and when combined with a hydrocarbon adsorption material in a trap, the exhaust temperature does not exceed 700° C.

ELIMINATION OF GASEOUS REACTANTS IN LITHIUM ION BATTERIES

A lithium ion battery is provided that includes a positive electrode, a negative electrode, and a separator disposed between the positive electrode and the negative electrode. One or more of the separator, positive electrode, and negative electrode includes a transition metal compound capable of catalyzing any gaseous reactants formed in the lithium ion battery to form a liquid. The transition metal compound may include ruthenium (Ru). In certain variations, the lithium ion battery includes an electrolyte that is a conductive medium for lithium ions to move between the positive electrode and the negative electrode. The electrolyte comprises a transition metal compound capable of catalyzing a reaction of any gaseous reactants to form a liquid. 1. A lithium ion battery comprising:a positive electrode;a negative electrode; anda separator disposed between the positive electrode and the negative electrode, wherein one or more of the separator, positive electrode, and negative electrode comprises a transition metal compound capable of catalyzing any gaseous reactants formed in the lithium ion battery to form a liquid.2. The lithium ion battery according to claim 1 , wherein the gaseous reactants are selected from the group consisting of: methane claim 1 , hydrogen claim 1 , carbon monoxide claim 1 , carbon dioxide claim 1 , ethylene claim 1 , ethane claim 1 , and combinations thereof.3. The lithium ion battery according to claim 1 , wherein the gaseous reactants comprise hydrogen chloromethane.4. The lithium ion battery according to claim 1 , wherein the transition metal compound comprises an element selected from the group consisting of:ruthenium (Ru), titanium (Ti), molybdenum (Mo), nickel (Ni), cobalt (Co), palladium (Pd), iridium (Ir), and combinations thereof.5. The lithium ion battery according to claim 4 , wherein the transition metal compound comprises ruthenium (Ru).6. The lithium ion battery according to claim 1 , wherein one of the positive electrode claim 1 , ...

BIMETALLIC CATALYSTS FOR SELECTIVE AMMONIA OXIDATION

Catalysts, methods, and systems for treating diesel engine exhaust streams are described. In one or more embodiments, the catalyst comprises a molecular sieve having a silica to alumina ratio (SAR) less than about 30, the molecular sieve including ion-exchanged copper and ion-exchanged platinum. Systems including such catalysts and methods of treating exhaust gas are also provided. 120.-. (canceled)21. A catalyst for oxidizing ammonia to nitrogen and NOx , the catalyst comprising an aluminosilicate molecular sieve having a silica-to-alumina ratio (SAR) less than 30 , the molecular sieve comprising ion-exchanged copper and ion-exchanged platinum , wherein the molecular sieve comprises a zeolite having a crystal framework type selected from FAU , MFI , MOR , BEA , HEU , and OFF , and wherein the catalyst is obtainable by a process comprising:(a) ion-exchange of copper on the molecular sieve,(b) calcination of the molecular sieve obtained in (a), and(c) ion-exchange of platinum on the molecular sieve obtained in (b).22. The catalyst of claim 21 , further comprising an amount of metallic platinum.23. The catalyst of claim 22 , wherein the aluminosilicate molecular sieve comprises a zeolite having a crystal framework type selected from FAU claim 22 , MFI claim 22 , MOR and BEA.24. The catalyst of claim 21 , wherein the aluminosilicate molecular sieve comprises a zeolite having a crystal framework type FAU and the zeolite has a SAR less than 10.25. The catalyst of claim 21 , wherein the aluminosilicate molecular sieve comprises a zeolite having a crystal framework type FAU and the zeolite has a SAR less than 6.26. The catalyst of claim 21 , wherein the catalyst is coated on a refractory ceramic support.27. The catalyst of claim 26 , wherein the total loading of the molecular sieve in the substrate is in the range of 18.3 g/1l (0.3 g/in3) and 183 g/1l (3.0 g/in3) claim 26 , based on the total catalyst volume.28. The catalyst of claim 21 , wherein the platinum particle size ...

Aromatization Processes Using Both Fresh and Regenerated Catalysts, and Related Multi-Reactor Systems

Multi-reactor systems with aromatization reactor vessels containing a catalyst with low surface area and pore volume, followed in series by aromatization reactor vessels containing a catalyst with high surface area and pore volume, are disclosed. Related reforming methods using the different aromatization catalysts also are described. 111-. (canceled)12. An aromatization reactor vessel system comprising:(A) at least one first reactor vessel comprising:(a1) a first reactor inlet for introducing a first hydrocarbon feed into the at least one first reactor vessel;(a2) a first aromatization catalyst for catalytically converting at least a portion of the first hydrocarbon feed under first reforming conditions to produce a first aromatic product; wherein the first aromatization catalyst comprises a first transition metal and a first catalyst support, the first aromatization catalyst characterized by:{'sup': 2', '2, 'a first surface area in a range from about 80 m/g to about 150 m/g; and/or'}a first micropore volume in a range from about 0.01 cc/g to about 0.048 cc/g; and(a3) a first reactor outlet for discharging a first effluent comprising the first aromatic product from the at least one first reactor vessel;(B) at least one second reactor vessel comprising:(b1) a second reactor inlet for introducing a second hydrocarbon feed into the at least one second reactor vessel;(b2) a second aromatization catalyst for catalytically converting at least a portion of the second hydrocarbon feed under second reforming conditions to produce a second aromatic product; wherein the second aromatization catalyst comprises a second transition metal and a second catalyst support, the second aromatization catalyst characterized by:{'sup': 2', '2, 'a second surface area in a range from about 160 m/g to about 260 m/g; and/or'}a second micropore volume in a range from about 0.05 cc/g to about 0.09 cc/g; and(b3) a second reactor outlet for discharging a second effluent comprising the second ...

PROCESSES AND CATAYLST SYSTEMS FOR PRODUCING MONOETHANOLAMINE FROM GLYCOLALDEHYDE

Improvements in catalyst systems and associated processes for the conversion of glycolaldehyde to monoethanolamine are disclosed. The catalyst systems exhibit improved selectivity to this desired product and consequently reduced selectivity to byproducts such as diethanolamine and ethylene glycol. These beneficial effects are achieved through the use of acids, and particularly Lewis acids, as co-catalysts of the reductive amination reaction, in conjunction with a hydrogenation catalyst.

A METHOD OF TREATING A ZEOLITE WITH AN ALUMINUM COMPOUND TO PREPARE A CATALYST FOR THE PRODUCTION OF AROMATICS AND THE CATALYST MADE THEREFROM

In an embodiment, a process of making a catalyst can comprise contacting a zeolite with an aluminum solution comprising an aluminum compound at a pH of 2 to 6; calcining the zeolite to form the catalyst; wherein the catalyst comprises 0.1 to 5 wt % aluminum based on the total weight of the catalyst excluding any binder or extrusion aide. In an embodiment, a process of aromatizing methane can comprise aromatizing a feed comprising methane in the presence of the catalyst under aromatization conditions.

Honeycomb structure

A honeycomb structure has grooves dented inwardly from the surfaces of the partition walls along a cell direction An open width of an open end of the groove is 0.015-0.505 mm and smaller than the open width a length of one side of each of the cells with the grooves, a bottom width of a bottom of the groove is 0.01-0.5 mm and smaller than the open width, a height from the bottom of the groove to the open end is 0.01-0.05 mm, a thickness of the partition wall in a groove portion is 50 μm or more, a ratio of the number of the cells with the grooves to the number of the total cells is 80% or more, and a value obtained by subtracting the open frontal area when the grooves excluded from the open frontal area when the grooves included is 0.1-8.0%.

Exhaust purification filter

Provided is a GPF capable of exhibiting better than conventional three-way purification function. A gasoline particulate filter (GPF) that is provided in an exhaust pipe of an engine and that performs purification by capturing particulate matter (PM) in exhaust gas is provided with a filter substrate in which a plurality of cells extending from an exhaust gas inflow-side end face to an outflow-side end face are defined by porous partition walls and in which openings at the inflow-side end face and openings at the outflow-side end face of the cells are alternately sealed; and a three-way catalyst (TWC) supported by the partition wall. The three-way catalyst is the GPF comprising a catalytic metal containing at least Rh, and a composite oxide having an oxygen storage capacity and containing Nd and Pr in a crystal structure.

Low-Temperature Oxidation Catalyst With Particularly Marked Hydrophobic Properties ForThe Oxidation Of Organic Pollutants

The present invention relates to a catalyst comprising a macroporous noble metal-containing zeolite material and a porous SiO-containing binder, wherein the catalyst has a proportion of micropores of more than 70%, based on the total pore volume of the catalyst. The invention is additionally directed to a process for preparing the catalyst and to the use of the catalyst as an oxidation catalyst. 112-. (canceled)13. A method of purifying exhaust , the method comprising:providing an exhaust gas containing an organic pollutant; a microporous noble metal-containing zeolite material, the zeolite material having less than 2 mol. % aluminium, the zeolite material being selected from zeolites of the types AFI, AEL, BEA, CHA, EUO, FAU, FER, KFI, LTL, MAZ, MOR, MEL, MTW, OFF, TON and MFI, the noble metal being selected from the group consisting of rhodium, iridium, palladium, platinum, ruthenium, osmium, gold and silver and combinations thereof; and', {'sub': '2', 'a porous SiO-containing binder having less than 0.04 wt % aluminium,'}, 'wherein the catalyst has a proportion of micropores having a diameter of less than 1 nm of more than 70% relative to the total pore volume of the catalyst., 'oxidizing the exhaust gas with a catalyst under conditions sufficient to oxidize the organic pollutant, the catalyst comprising'}14. The method according to claim 13 , wherein the exhaust gas is an exhaust gas from a combustion process.15. The method according to claim 13 , wherein the exhaust gas is an exhaust gas from a power plant.16. The method according to claim 13 , wherein the exhaust gas is an exhaust gas from an industrial process.17. The method according to claim 13 , wherein the oxidation is performed at a temperature below 300° C.18. The method according to claim 13 , wherein the organic pollutant is a solvent-type organic pollutant.19. The method according to claim 13 , wherein the organic pollutant is a paraffin claim 13 , an olefin claim 13 , an aldehyde or an aromatic.20. ...

Manganese-Containing Diesel Oxidation Catalyst

An oxidation catalyst composite, methods, and systems for the treatment of exhaust gas emissions from a diesel engine are described. More particularly, an oxidation catalyst composite including a first washcoat layer comprising a Pt component and a Pd component, and a second washcoat layer including a refractory metal oxide support containing manganese, a zeolite, and a platinum component is described.

MULTIPLE ZEOLITE HYDROCARBON TRAPS

Hydrocarbon (HC) traps are disclosed. The HC trap may include a first zeolite material having an average pore diameter of at least 5.0 angstroms and configured to trap hydrocarbons from an exhaust stream and to release at least a portion of the trapped hydrocarbons at a temperature of at least 225° C. The HC trap may also include a second zeolite material having an average pore diameter of less than 5.0 angstroms or larger than 7.0 angstroms. One or both of the zeolite materials may include metal ions, such as transition, Group 1A, or platinum group metals. The HC trap may include two or more discrete layers of zeolite materials or the two or more zeolite materials may be mixed. The multiple zeolite HC trap may form coke molecules having a relatively low combustion temperature, such as below 500° C. 1. A hydrocarbon trap , comprising:a first zeolite material having an average pore diameter of at least 5.0 angstroms and configured to trap hydrocarbons from an exhaust stream and to release at least a portion of the trapped hydrocarbons at a temperature of at least 225° C.; anda second zeolite material having an average pore diameter of less than 5.0 angstroms or larger than 7.0 angstroms.2. The trap of claim 1 , wherein the second zeolite material is configured to react with the hydrocarbons that are released from the first zeolite material to form coke molecules.3. The trap of claim 2 , wherein the second zeolite material is configured to form coke molecules having a combustion temperature of less than 500° C.4. The trap of claim 1 , wherein the first zeolite material is a beta (BEA) claim 1 , mordenite (MOR) or ZSM-5 (MFI) type zeolite.5. The trap of claim 1 , wherein the second zeolite material is a chabazite (CHA) claim 1 , ferrierite (FER) claim 1 , or ultra-stable Y (FAU) type zeolite.6. The trap of claim 1 , wherein the first zeolite material has a Si/Alratio of 20-50.7. The trap of claim 1 , wherein the first zeolite material includes from 0.1 to 10 wt. % ...

CATALYST DESIGN FOR HEAVY-DUTY DIESEL COMBUSTION ENGINES

Disclosed are washcoats, coated substrates formed from such washcoats, and catalytic converters for use in diesel applications, such as heavy duty diesel applications. Methods of preparing the coated substrates are also disclosed. 196-. (canceled)97. A coated substrate comprising:a) a substrate;b) a first washcoat layer on the substrate comprising zeolites;c) a second washcoat layer on the substrate comprising a first catalytically active material comprising platinum and palladium, wherein the first catalytically active material comprises first composite nanoparticles embedded within porous micron-sized carrier particles; wherein the first composite nanoparticles comprises a first support nanoparticle and a first catalytic nanoparticle, wherein the first catalytic nanoparticle comprises a platinum-palladium alloy; andd) a third washcoat layer on the substrate comprising a second catalytically active material comprising platinum and palladium; wherein the second catalytically active material comprises second composite nanoparticles embedded within porous micron-sized carrier particles; wherein the second composite nanoparticles comprises a second support nanoparticle and a second catalytic nanoparticle, wherein the second catalytic nanoparticle comprises a platinum-palladium alloy;wherein the second washcoat layer is deposited on the first washcoat layer, and the third washcoat layer is deposited on the second washcoat layer.98. The coated substrate of claim 97 , wherein the platinum-palladium alloy of the first catalytic nanoparticle comprises a platinum:palladium ratio of less than about 4:1 Pt:Pd.99. The coated substrate of claim 98 , wherein the platinum-palladium alloy of the first catalytic nanoparticle comprises a platinum:palladium ratio of about 1:1 to about 4:1 Pt:Pd.100. The coated substrate of claim 97 , wherein the platinum-palladium alloy of the second catalytic nanoparticle comprises a platinum:palladium ratio of greater than about 4:1 Pt:Pd.101. The ...

Process for removing oxidisable gaseous compounds from a gas mixture by means of a platinum-containing oxidation catalyst

Process for catalytic oxidative removal of at least one oxidisable gaseous compound from a gas mixture comprising the at least one oxidisable gaseous compound as well as oxygen through the use of an oxidation catalyst, whereby the gas mixture is not a combustion flue gas, characterised in that the oxidation catalyst was produced through the use of at least one exothermic-decomposing platinum precursor.

PROCESSES FOR ISOMERIZING ALPHA OLEFINS

Processes are described for isomerizing one or more C-Calpha olefins to produce an isomerization mixture comprising one or more C-Cinternal olefins comprising contacting an olefinic feed comprising the one or more C-Calpha olefins with a catalyst under isomerization conditions, wherein the catalyst comprises a microporous crystalline aluminosilicate selected from the group consisting of ZSM-5, ZSM-23, ZSM-35, ZSM-11, ZSM-12, ZSM-48, ZSM-57, and mixtures or combinations thereof, and wherein the microporous crystalline aluminosilicate has a SiO/AlOmolar ratio of less than or equal to about 100. The resulting isomerization mixture typically exhibits a lower pour point and maintained biodegradability properties as compared to the olefinic feed, and is particularly useful in drilling fluid and paper sizing compositions.

PASSIVE NOx ADSORBER

A NOx absorber catalyst for treating an exhaust gas from a diesel engine. The NOx absorber catalyst comprises a first region comprising a NOx absorber material comprising a molecular sieve catalyst, and a second region comprising a nitrogen dioxide reduction material; and a substrate having an inlet end and an outlet end.

METHOD FOR FORMING LIGHT OLEFINS FROM METHANOL

A catalyst system and a process for methanol to light olefin conversion with enhanced selectivity towards propylene. The catalyst system comprises a honeycomb monolith catalyst support coated with aluminosilicate nanozeolite catalysts on the edges and inside the channels of the support structure. The aluminosilicate nanozeolite catalysts have not been pre-modified with a promoter metal. The catalyst system gives higher hydrothermal stability to the catalyst compared to randomly packed pellet catalysts and allows methanol to be converted to predominantly propylene at a low temperature, with decreased selectivity towards C, higher olefins and paraffinic hydrocarbons. 1: A method for forming light olefins from methanol , comprising:contacting gaseous methanol with a catalyst system for a time and at a temperature effective for converting the methanol to propylene and for forming a light olefin mixture,wherein the contacting is carried out with a selectivity towards converting methanol to propylene of at least 40% relative to a total mass of the light olefin mixture and a selectivity towards forming propylene is greater than a selectivity towards forming ethylene relative to a total mass of the light olefin mixture and that is greater than a selectivity towards forming butylene relative to a total mass of the light olefin mixture, 7-12 wt % of the zeolite nanoparticles relative to the total weight of the catalyst system of zeolite nanoparticles having a silica to alumina molar ratio of 260-5000 in the form of crystals having an average particle diameter of 10-50 nm; and', 'a honeycomb monolith support with 500-1200 cells per square inch coated with the zeolite nanoparticles on the edges and inside the channels of the honeycomb monolith support;', 'wherein the zeolite nanoparticles are not modified with a promoter metal., 'wherein the catalyst system comprises2: The method of claim 1 , wherein the zeolite nanoparticles are microporous molecular sieves having an MFI ...

CATALYTIC ARTICLES

Catalytic articles comprising a substrate having a catalytic coating thereon, the catalytic coating comprising a catalytic layer having a thickness and an inner surface proximate to the substrate and an outer surface distal to the substrate; where the catalytic layer comprises a noble metal component on support particles and where the concentration of the noble metal component towards the outer surface is greater than the concentration towards the inner surface are highly effective towards treating exhaust gas streams of internal combustion engines. The articles are prepared via a method comprising providing a first mixture comprising micron-scaled support particles and applying the first mixture to a substrate to form a micro-particle layer; providing a second mixture comprising nano-scaled support particles and a noble metal component having an initial pH and applying the second mixture to the micro-particle layer and calcining the substrate. 1. A catalytic article comprising: a catalytic layer having a thickness, an inner surface proximate to the substrate and an outer surface distal to the substrate,', 'wherein the catalytic layer comprises a noble metal component on support particles and wherein the concentration of the noble metal component towards the outer surface is greater than the concentration towards the inner surface., 'a substrate having a catalytic coating thereon, the catalytic coating comprising2. A catalytic article according to claim 1 , wherein at least 50 wt % of the noble metal component resides in the outer one fifth of the thickness of the catalytic layer.3. A catalytic article according to claim 1 , wherein at least 70 wt % of the noble metal component resides in the outer one half of the thickness of the catalytic layer.4. A catalytic article according to claim 1 , wherein where ≥80 wt % of the noble metal resides in the outer 20% of the thickness of the catalytic layer.5. A catalytic article according to claim 1 , wherein the noble metal ...

NITROGEN OXIDES AND HYDROCARBON STORAGE CATALYST AND METHODS OF USING THE SAME

A nitrogen oxides (NO) and hydrocarbon (HC) storage catalyst for treating an exhaust gas flow is provided. The NOand HC storage catalyst includes (a) a zeolite, (b) noble metal atoms, and (c) a metal oxide, a non-metal oxide, or a combination thereof. One or more of the noble metal atoms is present in a complex with the metal oxide, the non-metal oxide or a combination thereof. The complex is dispersed within a cage of the zeolite. Methods of preparing the NOand HC storage catalyst and methods of using the NOand HC storage catalyst for treating an exhaust gas stream flowing from a vehicle internal combustion engine during a period following a cold-start of the engine are also provided. 1. A nitrogen oxides (NO) and hydrocarbon (HC) storage catalyst for treating an exhaust gas flow comprising:(a) a zeolite comprising a cage and having a framework structure selected from the group consisting of BEA, MFI, CHA, AEI, EMT, ERI, MOR, MER, FER, FAU, LEV, MWW, CON, EUO, and combinations thereof;(b) noble metal atoms selected from the group consisting of Pd atoms, Pt atoms, Rh atoms, Ag atoms, Ru atoms, Au atoms, Ir atoms and combinations thereof; and(c) a metal oxide, a non-metal oxide, or a combination thereof, wherein the metal of the metal oxide is selected from the group consisting of alkali metals, alkaline earth metals, transitions metals, lanthanides, and combinations thereof and the non-metal of the non-metal oxide is phosphorus; andwherein one or more of the noble metal atoms are present in a complex with: (i) the metal oxide; (ii) the non-metal oxide; or (iii) the metal oxide and the non-metal oxide; and wherein the complex is dispersed within the cage of the zeolite.2. The storage catalyst of claim 1 , wherein the noble metal atoms are present in an amount of about 0.1 wt. % to about 10 wt. % based on total weight of the NOand HC storage catalyst.3. The storage catalyst of claim 1 , wherein the metal oxide claim 1 , the non-metal oxide claim 1 , or a combination ...

CATALYTIC ARTICLES

Catalytic articles comprising a substrate having a catalytic coating thereon, the catalytic coating comprising a catalytic layer having a thickness and an inner surface proximate to the substrate and an outer surface distal to the substrate; where the catalytic layer comprises a noble metal component on support particles and where the concentration of the noble metal component towards the outer surface is greater than the concentration towards the inner surface are highly effective towards treating exhaust gas streams of internal combustion engines. The articles are prepared via a method comprising providing a first mixture comprising micron-scaled support particles and applying the first mixture to a substrate to form a micro-particle layer; providing a second mixture comprising nano-scaled support particles and a noble metal component having an initial pH and applying the second mixture to the micro-particle layer and calcining the substrate. 111-. (canceled)12. A method of treating an exhaust stream of an internal combustion engine comprising contacting the exhaust stream with a catalytic article comprising: a catalytic layer having a thickness, an inner surface proximate to the substrate, and an outer surface distal to the substrate,', 'wherein the catalytic layer comprises a noble metal component on support particles, and wherein the concentration of the noble metal component towards the outer surface is greater than the concentration towards the inner surface., 'a substrate having a catalytic coating thereon, the catalytic coating comprising13. A method of making a catalytic article comprising:providing a first mixture comprising micron-scaled support particles and applying the first mixture to a substrate to form a micro-particle layer;providing a second mixture comprising nano-scaled support particles and a noble metal component having an initial pH and applying the second mixture to the micro-particle layer; andcalcining the substrate.14. The method ...

EXHAUST EMISSION REDUCTION SYSTEM HAVING AN HC-TRAP AND NOX-TRAP COMBINATION DESIGNED FOR OPERATING UNDER STRATEGIC LEAN CONDITIONS

Methods and systems are featured for reducing harmful exhaust gas components of combustion devices such as gasoline-powered combustion engines (e.g., predominately stoichiometric running engines). The methods and systems include an underbody combination of a hydrocarbon trap (HCT), suited for cold start hydrocarbon adsorption, as well as an associated NOx trap. The system is inclusive of a control unit for extending a lean exhaust condition reaching the desorbing HCT as to avoid a deficiency in oxygen during the time period of HCT desorption. The system is also inclusive of one or more TWCs as in one associated with the underbody HCT-NOx-trap combination and/or one positioned in a close coupled position. Platinum group metals as in Pd, Rh and Pt are also featured on one, two or all three of the HCT, NOx-trap, and TWC when present. 1. An exhaust emission reduction system suited for use with a gasoline running engine , comprising:an exhaust treatment apparatus having an underbody positioned NOx-trap and HC-trap combination;a control unit operable to extend a lean exhaust condition into a period of desorption of hydrocarbons trapped by the HC-trap as to promote hydrocarbon emission reduction during the desorption period.2. The system of wherein the NOx-trap and HC-trap combination includes a substrate support onto which the HC-trap is layered and over which HC-trap layer the NOx-trap is layered.3. The system of wherein the exhaust treatment apparatus further comprises one or more TWC components.4. The system of wherein the exhaust treatment apparatus comprises both an upstream close coupled TWC component and a downstream claim 3 , underbody TWC component claim 3 , with the downstream TWC being in a common support canister with NOx-trap and HC-trap components of the NOx-trap and HC-trap combination.5. The system of wherein the NOx-trap and HC-trap combination includes a substrate support onto which the HC-trap is layered and over which HC-trap layer the NOx-trap is ...

ZEOLITE MEMBRANE STRUCTURE AND METHOD FOR PRODUCING SAME

A zeolite membrane structure includes a porous support, and a zeolite membrane. The zeolite membrane has a first zeolite layer located in a surface of the porous support, and a second zeolite layer located outside of the surface of the porous support and integrally formed with the first zeolite layer. The porous support has an outermost layer in which the first zeolite layer is located. An average thickness of the first zeolite layer is less than or equal to 5.4 micrometers. An average pore diameter of the outermost layer is greater than or equal to 0.050 micrometers and less than or equal to 0.150 micrometers. 1. A zeolite membrane structure comprising:a porous support, anda zeolite membrane, andthe zeolite membrane having a first zeolite layer located in a surface of the porous support, and a second zeolite layer located outside of the surface of the porous support and integrally formed with the first zeolite layer,the porous support having an outermost layer in which the first zeolite layer is located,an average thickness of the first zeolite layer being less than or equal to 5.4 micrometers, anda 50% diameter in a volume-accumulated pore diameter distribution of the outermost layer measured by use of a pore diameter distribution measurement apparatus being greater than or equal to 0.050 micrometers and less than or equal to 0.150 micrometers.2. The zeolite membrane structure according to claim 1 , wherein a ratio of an average thickness of the first zeolite layer to an average thickness of the second zeolite layer is less than or equal to 2.0.3. The zeolite membrane structure according to claim 1 , wherein an average thickness of the first zeolite layer is less than or equal to 2.5 micrometers.4. A method of manufacturing a zeolite membrane structure comprising:coating a slurry for seeding containing a zeolite seed crystals on a surface of a porous support, andcausing crystal growth of the zeolite seed crystals, and whereina ratio of a 10% diameter in a volume- ...

Oxidation catalyst for internal combustion engine exhaust gas treatment

The invention provides an exhaust gas cleaning oxidation catalyst and in particular to an oxidation catalyst for cleaning the exhaust gas discharged from internal combustion engines of compression ignition type (particularly diesel engines). The invention further relates to a catalysed substrate monolith comprising an oxidising catalyst on a substrate monolith for use in treating exhaust gas emitted from a lean-burn internal combustion engine. In particular, the invention relates to a catalysed substrate monolith comprising a first washcoat coating and a second washcoat coating, wherein the second washcoat coating is disposed in a layer above the first washcoat coating.

PASSIVE NITROGEN OXIDE ADSORBER

The present invention relates to a catalyst, comprising a carrier substrate of the length (L) which extends between two carrier substrate ends (a and b) and has two coating zones (A and B), wherein the coating zone (A) comprises a zeolite and palladium and, proceeding from the carrier substrate end (a), extends on a part of the length (L), the coating zone (B) comprises the same components as coating zone (A) and platinum and, proceeding from the carrier substrate end (b), extends on a part of the length (L), wherein L=L+L, wherein LA denotes the length of the coating zone (A) and Ldenotes the length of the coating zone (B). The invention also relates to an exhaust system containing said catalyst. 1. Catalyst comprising a carrier substrate of length L , which extends between two carrier substrate ends a and b and comprises two coating zones A and B , whereincoating zone A comprises a zeolite and palladium and extends from carrier substrate end a along a part of length L,coating zone B comprises the same components as coating zone A and platinum and extends starting from carrier substrate end b along a part of length L, wherein{'sub': A', 'B', 'A', 'B, 'L=L+Lapplies, wherein Lis the length of the coating zone A and Lis the length of the coating zone B.'}2. Catalyst according to claim 1 , characterized in that the largest channels of the zeolite are formed by 6 tetrahedrally coordinated atoms and the zeolite belongs to structure types AFG claim 1 , AST claim 1 , DOH claim 1 , FAR claim 1 , FRA claim 1 , GIU claim 1 , LIO claim 1 , LOS claim 1 , MAR claim 1 , MEP claim 1 , MSO claim 1 , MTN claim 1 , NON claim 1 , RUT claim 1 , SGT claim 1 , SOD claim 1 , SVV claim 1 , TOL or UOZ.3. Catalyst according to claim 1 , characterized in that the largest channels of the zeolite are formed by 8 tetrahedrally coordinated atoms and the zeolite belongs to structure types ABW claim 1 , ACO claim 1 , AEI claim 1 , AEN claim 1 , AFN claim 1 , AFT claim 1 , AFV claim 1 , AFX claim 1 ...

EXHAUST GAS PURIFICATION SYSTEM

An exhaust gas purifier is disposed in an exhaust gas passage of an engine, and includes: a DPF for capturing PM contained in exhaust gas; an SCR catalyst provided downstream of the DPF in a direction of flow of the exhaust gas, and for reducing NOcontained in the exhaust gas for purification in the presence of NH; an inj ection unit provided between the DPF and the SCR catalyst, and for supplying urea to the SCR catalyst so as to supply NHto the SCR catalyst; and an AMOX provided downstream of the SCR catalyst in the direction of flow of the exhaust gas, and for removing NHhaving passed through the SCR catalyst. The DPF does not contain Pt or Pd, and contains Rh. The AMOX contains Pt. 1. An exhaust gas purification system disposed in an exhaust gas passage of an engine , comprising:a particulate filter configured to capture particulates contained in exhaust gas;{'sub': 'x', 'an SCR catalyst provided downstream of the particulate filter in a direction of flow of the exhaust gas, and configured to reduce NOcontained in the exhaust gas for purification in the presence of a reducing agent;'}an injection unit provided between the particulate filter and the SCR catalyst, and configured to supply the reducing agent or a precursor of the reducing agent to the SCR catalyst so as to supply the reducing agent to the SCR catalyst; anda reducing agent oxidation catalyst provided downstream of the SCR catalyst in the direction of flow of the exhaust gas, and configured to remove the reducing agent having passed through the SCR catalyst, whereinthe particulate filter contains a Zr-based composite oxide which does not contain a catalytic noble metal or Ce, and a Rh-doped Ce-containing Zr-based composite oxide, and does not contain Pt or Pd as a catalytic noble metal, and the reducing agent oxidation catalyst contains Pt.2. The exhaust gas purification system of claim 1 , whereinthe amount of Pt contained in the reducing agent oxidation catalyst is 0.1-6.0 g/L with respect to the ...

Zeolite catalysts having stabilized hydrogenation-dehydrogenation function

A zeolite catalyst suitable for use in shape-selective hydrocarbon conversion processes. The catalyst is modified by incorporation therein of a hydrogenation-dehydrogenation functional metal, followed by gradient selectivation with an organosilicon compound under conversion conditions, wherein the gradient selectivation conditions are characterized by a progressive temperature gradient. The use of a progressive temperature gradient during the in situ selectivation procedure unexpectedly yields a catalyst in which the hydrogenation-dehydrogenation function is stabilized, thereby enabling long duration hydrocarbon conversion processes with low by-product make.

Zeolite catalysts having stabilized hydrogenation-dehydrogenation function

A zeolite catalyst suitable for use in shape-selective hydrocarbon conversion processes. The catalyst is modified by incorporation therein of a hydrogenation-dehydrogenation functional metal, followed by gradient selectivation with an organosilicon compound under conversion conditions, wherein the gradient selectivation conditions are characterized by a progressive temperature gradient. The use of a progressive temperature gradient during the in situ selectivation procedure unexpectedly yields a catalyst in which the hydrogenation-dehydrogenation function is stabilized, thereby enabling long duration hydrocarbon conversion processes with low by-product make.

Catalyst useful for simultaneous removal of carbon monoxide and hydrocarbons from oxygen-rich gases comprises tin oxide and palladium loaded on carrier oxide

Catalyst comprises tin oxide and palladium loaded on carrier oxide in a roentgenographically amorphous or a nanoparticular form. Independent claims are included for the following: (1) process for manufacturing of catalyst involving bringing tin compounds and palladium compounds into contact with a carrier oxide; (2) a process for removal of harmful substances from exhaust gases of lean combustion engines by using a catalyst involving oxidation of carbon monoxide and hydrocarbons as well as the simultaneous removal of carbon black particles by oxidation.

Catalyst for purifying diesel engines exhaust gases and process for its preparation

Process to prepare a catalyst for exhaust gas purification

Adsorbent comprising sepiolite and zeolite

Adsorbent comprising a sepiolite in amount of 90-10 wt.% and a zeolite in amount of 10-90 wt.% such as chabazite, mordenite, erionite, faujasite, clinoptilolite zeolites A, X, Y, omega, ZSM-5 or silicalite. The adsorbent may include a catalyst eg. a metal element, an oxide or a complex compound of at least one metal selected from the platinum group metals eg: Rh, Pd, Os, Im, Pt; the iron group metals eg: Fe, Co, Ni; group metals eg: Cu, Ag; group VII metals eg: Mn and rare earths eg: Ce, La or a combination thereof. The adsorbent is used as a deodorizer and/or to catalytically decompose the adsorbates during adsorbent regeneration.

Process of synthesis gas conversion to liquid fuels using mixture of synthesis gas conversion catalyst and dual functionality catalyst

A process is disclosed for converting a feed comprising synthesis gas to liquid hydrocarbons within a single reactor at essentially common reaction conditions. The synthesis gas contacts a catalyst bed comprising a mixture of a synthesis gas conversion catalyst on a support containing an acidic component and a dual functionality catalyst including a hydrogenation component and a solid acid component. The hydrocarbons produced are liquid at about 0° C., contain at least 25% by volume C 10+ and are substantially free of solid wax.

Process of synthesis gas conversion to liquid hydrocarbon mixtures using a catalyst system containing ruthenium and an acidic component

The disclosure relates to a method of performing a synthesis gas conversion reaction in which synthesis gas contacts a catalyst system including a mixture of ruthenium loaded Fischer-Tropsch catalyst particles and at least one set of catalyst particles including an acidic component promoted with a noble metal, e.g., Pt or Pd. The reaction occurs at conditions resulting in a hydrocarbons product containing 1-15 weight % CH 4 , 1-15 weight % C 2 -C 4 , 70-95 weight % C 5+ , 0-5 weight % C 21+ normal paraffins, and 0-10 weight % aromatic hydrocarbons.

Metal zeolite catalyst preparation

Zeolite-metal catalysts having a substantial amount of catalytically active metal, e.g. iron, deposited in the cavities of the zeolite in zero-valent, small cluster form, are prepared by vaporizing the metal under low vapor pressure conditions in the vicinity of an organic liquid solvent, e.g. toluene, such that the metal dissolves in the solvent as a labile solvated zero-valent metal complex. This complex is contacted with the zeolite so that the complex diffuses into the cavities of the zeolite. Upon subsequent warming the solvated metal complex decomposes, leaving zero-valent small metal clusters in the zeolite cavities.

Metal zeolite catalyst preparation

Process and catalyst for converting synthesis gas to liquid hydrocarbon mixture

Synthesis gas containing CO and H 2 is converted to a high-octane hydrocarbon liquid in the gasoline boiling point range by bringing the gas into contact with a heterogeneous catalyst including, in physical mixture, a zeolite molecular sieve, cobalt at 6-20% by weight, and thoria at 0.5-3.9% by weight. The contacting occurs at a temperature of 250°-300° C., and a pressure of 10-30 atmospheres. The conditions can be selected to form a major portion of the hydrocarbon product in the gasoline boiling range with a research octane of more than 80 and less than 10% by weight aromatics.

Modified zeolite catalyst useful for the conversion of paraffins, olefins and aromatics in a mixed feedstock into isoparaffins and a process thereof

The invention relates to a modified zeolite catalyst, useful for the conversion of paraffins, olefins and aromatics in a mixed feedstock such as FCC gasoline that contain high content of olefin, aromatic and n-paraffin into isoparaffins. The invention further relates to the use of such a catalyst, for example but not limited to, in a process for the conversion of paraffins, olefins and aromatics in a mixed feedstock into the product having high amount of branched paraffins with decreased aromatics and olefins, a useful gasoline blend, with negligible production of lighter gases.

Process of synthesis gas conversion to liquid fuels using mixture of synthesis gas conversion catalyst and dual functionality catalyst

A process is disclosed for converting a feed comprising synthesis gas to liquid hydrocarbons within a single reactor at essentially common reaction conditions. The synthesis gas contacts a catalyst bed comprising a mixture of a synthesis gas conversion catalyst on a support containing an acidic component and a dual functionality catalyst including a hydrogenation component and a solid acid component. The hydrocarbons produced are liquid at about 0° C., contain at least 25% by volume C 10+ and are substantially free of solid wax.

Process for producing aromatic hydrocarbon compounds and liquefied petroleum gas from hydrocarbon feedstock

Fisclosed are a process for producing aromatic hydrocarbon compounds and liquefied petroleum gas (LPG) from a hydrocarbon feedstock having boiling points of 30-250 °C and a catalyst useful therefor. In the presence of said catalyst, aromatic components in the hydrocarbon feedstock are converted to BTX-enriched components of liquid phase through hydrodealkylation and/or transalkylation, and non-aromatic components are converted to LPG-enriched gaseous materials through hydrocracking. The products of liquid phase may be separated as benzene, toluene, xylene, and C9 or higher aromatic compounds, respectively according to their different boiling points, while LPG is separated from the gaseous products, in a distillation tower.

Catalyst for alkylation of lower olefin with iso-paraffin useful for producing high octane fuel additive

Catalyst for alkylation of 2-5C olefins with iso-paraffins to produce a high-octane fuel additive consists of 0.02-0.50 wt.% finely-divided group VIII metal on a highly porous, ion-exchanged crystalline aluminum silicate. Catalyst for alkylation of 2-5C olefins with iso-paraffins to produce a high-octane fuel additive consists of 0.02-0.50 wt.% finely-divided group VIII metal (with respect to the total weight of catalyst without support) on a highly porous, ion-exchanged crystalline aluminum silicate with composition of formula (I); REaMbNac((Al1Six)O2(1+x)).yH2O (I) RE = lanthanum or a lanthanide except cerium; M = an alkaline earth metal; a = 0.10-0.30; b = 0.05-0.25; c = 0.01-0.05; x = 1.0-3.0; y = 3.0-5.0 Independent claims are also included for (a) the alkylation process; and (b) the production of the catalyst. Used in the production of an additive, especially 8 carbon alkylate, for increasing the octane number of fuel.

Modified zeolite Y catalyst composition

A catalyst composition comprising a modified zeolite and a binder mixed with a high degree of mixing has high hydrothermal resistance and exhibits high activities in various catalytic reactions, including various hydrocarbon-conversion reactions, and the catalyst composition is prepared by mixing a slurry of a modified zeolite and a slurry of a binder material.

Catalyst for reduction of nitrogen oxides

A catalyst for the selective reduction of nitrogen oxides to nitrogen in the presence of ammonia in the form of composite bodies formed from a mixture of anatase (5 to 40% by weight), a zeolite (50 to 90%), a bond material (0 to 30%, and, optionally, promoter which is an oxide of vanadium, molybdenum, or copper, in the amount of at least 0.1% by weight.

Catalyst and process for converting methanol to hydrocarbons